Process Using Substituted Metallocene Catalysts and Products Therefrom

ABSTRACT

This invention relates to a process to produce propylene polymer using a bridged hafnium transition metal metallocene catalyst compounds having two indenyl ligands substituted at the 4 positions with a C 1  to C 10  alkyl, where the 3 positions are hydrogen (assuming the bridge position is counted as the one position) and the bridging atom is carbon or silicon which is incorporated into a cyclic group comprising 3, 4, 5, or 6 silicon and/or carbon atoms that make up the cyclic ring, where the propylene polymer has 1) greater than 40% vinyl chain ends, relative to the total unsaturated chain ends, 2) a Tm of 70° C. or more; an Mw of 3000 to 300,000 g/mol, and 4) a g′ vis  of 0.90 or less.

PRIORITY

This application claims priority to and the benefit of U.S. Ser. No.61/847,442, filed Jul. 17, 2013 and to U.S. Ser. No. 61/847,464, filedJul. 17, 2013.

FIELD OF THE INVENTION

This invention relates to the use of bridged hafnium metallocenecompounds comprising indenyl ligands substituted at the 4 positioncapable of producing vinyl terminated polymers and the polymers soproduced.

BACKGROUND OF THE INVENTION

Alpha-olefins, especially those containing about 6 to about 20 carbonatoms, have been used as intermediates in the manufacture of detergentsor other types of commercial products. Such alpha-olefins have also beenused as comonomers, especially in linear low density polyethylene.Commercially produced alpha-olefins are typically made by oligomerizingethylene. Longer chain alpha-olefins, such as vinyl-terminatedpolyethylenes are also known and can be useful as building blocksfollowing functionalization or as macromonomers.

Allyl terminated low molecular weight solids and liquids of ethylene orpropylene have also been produced, typically for use as branches inpolymerization reactions. See, for example, Rulhoff, Sascha andKaminsky, (“Synthesis and Characterization of Defined BranchedPoly(propylene)s with Different Microstructures by Copolymerization ofPropylene and Linear Ethylene Oligomers (C_(n)=26-28) withMetallocenes/MAO Catalysts,” Macromolecules, 16, 2006, pp. 1450-1460),and Kaneyoshi, Hiromu et al. (“Synthesis of Block and Graft Copolymerswith Linear Polyethylene Segments by Combination of DegenerativeTransfer Coordination Polymerization and Atom Transfer RadicalPolymerization,” Macromolecules, 38, 2005, pp. 5425-5435).

Further, U.S. Pat. No. 4,814,540 discloses bis(pentamethylcyclopentadienyl) hafnium dichloride, bis(pentamethyl cyclopentadienyl)zirconium dichloride and bis(tetramethyl n-butyl cyclopentadienyl)hafnium dichloride with methylalumoxane in toluene or hexane with orwithout hydrogen to make allylic vinyl terminated propylenehomo-oligomers having a low degree of polymerization of 2-10. Theseoligomers do not have high Mns and do not have at least 93% allylicvinyl unsaturation. Likewise, these oligomers lack comonomer and areproduced at low productivities with a large excess of alumoxane (molarratio 600 Al/M; M═Zr, Hf). Additionally, no less than 60 wt % solvent(solvent+propylene basis) is present in all of the examples.

Teuben, et al. (J. Mol. Catal., 62, 1990, pp. 277-287) discloses the useof [Cp*₂MMe(THT)]+[BPh₄] (M═Zr and Hf; Cp*=pentamethylcyclopentadienyl;Me=methyl, Ph=phenyl; THT=tetrahydrothiophene), to make propyleneoligomers. For M=Zr, a broad product distribution with oligomers up toC₂₄ (number average molecular weight (Mn) of 336) was obtained at roomtemperature. Whereas, for M=Hf, only the dimer 4-methyl-1-pentene andthe trimer 4,6-dimethyl-1-heptene were formed. The dominant terminationmechanism appeared to be beta-methyl transfer from the growing chainback to the metal center, as was demonstrated by deuterium labelingstudies.

X. Yang, et al. (Angew. Chem. Intl Ed. Engl., 31, 1992, pp. 1375)discloses amorphous, low molecular weight polypropylene made at lowtemperatures where the reactions showed low activity and product having90% allylic vinyls, relative to all unsaturations, by ¹H NMR.Thereafter, Resconi, et al. (J. Am. Chem. Soc., 114, 1992, pp.1025-1032), discloses the use ofbis(pentamethylcyclopentadienyl)zirconium andbis(pentamethylcyclopentadienyl)hafnium to polymerize propylene andobtained beta-methyl termination resulting in oligomers and lowmolecular weight polymers with “mainly allyl- and iso-butyl-terminated”chains. As is the case in U.S. Pat. No. 4,814,540, the oligomersproduced do not have at least 93% allyl chain ends, an Mn of about 500to about 20,000 g/mol (as measured by ¹H NMR), and the catalyst has lowproductivity (1-12,620 g/mmol metallocene/hr; >3000 wppm Al inproducts).

Similarly, Small and Brookhart, (Macromolecules, 32, 1999, pp. 2322)disclose the use of a pyridylbisamido iron catalyst in a low temperaturepolymerization to produce low molecular weight amorphous propylenematerials apparently having predominant or exclusive 2,1 chain growth,chain termination via beta-hydride elimination, and high amounts ofvinyl end groups.

Weng et al. (Macromol Rapid Comm. 2000, 21, pp. 1103-1107) disclosesmaterials with up to about 81% vinyl termination made usingdimethylsilyl bis(2-methyl, 4-phenyl-indenyl) zirconium dichloride andmethylalumoxane in toluene at about 120° C. The materials have a Mn ofabout 12,300 (measured with ¹H NMR) and a melting point of about 143° C.Markel et al. (Macromolecules, 33, 2000, pp. 8541-8548) discloses combbranch-block polyethylene made with Cp₂ZrCl₂ and(C₅Me₄SiMe₂NC₁₂H₂₃)TiCl₂, activated with methyl alumoxane.

Moscardi et al. (Organometallics, 20, 2001, pp. 1918) discloses the useof rac-dimethylsilylmethylenebis(3-t-butyl indenyl)zirconium dichloridewith methylalumoxane in batch polymerizations of propylene to producematerials where “ . . . allyl end group always prevails over any otherend groups, at any [propene].” In these reactions, morphology controlwas limited and approximately 60% of the chain ends are allylic.

Coates, et al. (Macromolecules, 38, 2005, pp. 6259) disclosespreparation of low molecular weight syndiotactic polypropylene([rrrr]=0.46-0.93) with about 100% allyl end groups usingbis(phenoxyimine)titanium dichloride ((PHI)₂TiCl₂) activated withmodified methyl alumoxane (MMAO; Al/Ti molar ratio=200) in batchpolymerizations run between −20° C. and +20° C. for four hours. Forthese polymerizations, propylene was dissolved in toluene to create a1.65 M toluene solution. Catalyst productivity was very low (0.95 to1.14 g/mmol Ti/hr).

JP 2005-336092 A2 discloses the manufacture of vinyl-terminatedpropylene polymers using materials such as H₂SO₄ treatedmontmorillonite, triethylaluminum, triisopropyl aluminum, where theliquid propylene is fed into a catalyst slurry in toluene. This processproduces substantially isotactic macromonomers that do not have asignificant amount of amorphous material.

U.S. Pat. No. 6,897,261 discloses olefin graft copolymers obtained bycopolymerizing an atactic branched macromonomer, wherein themacromonomer is derived from monomers selected from the group consistingof (1) propylene and (2) the combination of propylene and at least oneselected from ethylene, alpha-olefins having from 4 to 20 carbon atoms,cyclic olefins and styrenes, and of which the propylene content fallsbetween 0.1 mol % and 100 mol %, and which macromonomer satisfies thefollowing (a) and (b): (a) its weight-average molecular weight (Mw)measured through gel permeation chromatography (GPC) falls between 400and 200000; (b) its vinyl content is at least 70 mol % of all theunsaturated groups in the macromonomer, wherein the macromonomersatisfies each of the following (i), (ii), and (iii): (i) the ratio ofthe temperature dependency (E₂) of the macromonomer solution viscosityto the temperature dependency (E₁) of the solution viscosity of thelinear polymer which has the same type of monomer, the same chemicalcomposition and the same intrinsic viscosity as those of themacromonomer, E₂/E₁, satisfies the following relationship:1.0<E₂/E₁<2.5.

Rose et al. (Macromolecules, 41, 2008, pp. 559-567) disclosespoly(ethylene-co-propylene) macromonomers not having significant amountsof iso-butyl chain ends. Those were made with bis(phenoxyimine) titaniumdichloride ((PHI)₂TiCl₂) activated with modified methylalumoxane (MMAO;Al/Ti molar ratio range 150 to 292) in semi-batch polymerizations (30psi propylene added to toluene at 0° C. for 30 min, followed by ethylenegas flow at 32 psi of over-pressure at about 0° C. for polymerizationtimes of 2.3 to 4 hours to produce E-P copolymer having an Mn of about4,800 to 23,300. In four reported copolymerizations, allylic chain endsdecreased with increasing ethylene incorporation roughly according tothe equation:

% allylic chain ends (of total unsaturations)=−0.95(mol % ethyleneincorporated)+100.

For example, 65% allyl (compared to total unsaturation) was reported forE-P copolymer containing 29 mol % ethylene. This is the highest allylpopulation achieved. For 64 mol % incorporated ethylene, only 42% of theunsaturations are allylic. Productivity of these polymerizations rangedfrom 0.78×10² g/mmol Ti/hr to 4.62×10² g/mmol Ti/hr.

Prior to this work, Zhu, et al. (Macromolecules, 35, 2002, pp.10062-10070 and Macromolecules Rap. Commun., 24, 2003, pp. 311-315)reported only low (−38%) vinyl terminated ethylene-propylene copolymermade with the constrained geometry metallocene catalyst[C₅Me₄(SiMe₂N-tert-butyl)TiMe₂ activated with B(C₆F₅)₃ and MMAO.

Janiak and Blank summarize a variety of work related to oligomerizationof olefins (Macromol. Symp., 236, 2006, pp. 14-22).

U.S. Pat. No. 6,225,432 discloses branched polypropylene compositionswhich have improved melt strength and good processability. The branchedpolypropylene compositions have a polydispersity of less than 4.0 and amelt point greater than 90° C. The weight average branching index g ofthe polypropylene compositions is less than 0.95.

WO2012/134715 discloses a process to produce branched polypropylenecompositions containing long chain branching and allylic chain ends,however, few polymerization examples contain greater than 50% allylicchain ends, and high polymerization temperatures (130 C) were requiredto produce polypropylene with 83% allylic end groups (ex. 59).Additionally, higher than 50% allylic chain ends was only accomplishedwhen a very bulky activator was used. Use of the less bulky activator,dimethylanilinium tetrakis(pentafluorophenyl)borate produced polymerswith more vinylidene unsaturation vs.

vinyl unsaturation.

WO2009/155471,WO2012/134719, and WO2012/134720 discloses polypropylenehomopolymers and/or ethylene-propylene copolymers with high levels ofallylic chain ends, no crystallinity, and lower molecular weights. Thereis no mention of the polymers having long chain branching.

However, processes to make branched polyolefins having high amounts ofallyl terminations on a commercial scale are not known. Accordingly,there is a need for new processes that produce allyl terminated branchedpolyolefins that have allyl termination present in high amounts (50% ormore), particularly in high yields and with a wide range of molecularweights, that can be made at commercial rates (5,000 g/mmol/hrproductivity or more). There is further a need for branched polyolefinreactive materials having high amounts of allyl termination which can befunctionalized and used in additive applications or as blendingcomponents.

SUMMARY OF THE INVENTION

This invention relates to a process for polymerization, comprising: (i)contacting one or more monomers comprising propylene and optionallyethylene, with a catalyst system comprising a metallocene catalystcompound and an activator, wherein the metallocene catalyst compound isrepresented by the formula:

where each R³ is hydrogen; each R⁴ is independently a C₁-C₁₀ alkyl; eachR² and R⁷ is independently hydrogen, or C₁-C₁₀ alkyl, each R⁵ and R⁶ isindependently hydrogen, C₁-C₅₀ substituted or unsubstituted hydrocarbyl,or C₁-C₅₀ substituted or unsubstituted halocarbyl; and R⁴ and R⁵, R⁵ andR⁶ and/or R⁶ and R⁷ may optionally be bonded together to form a ringstructure; J is a bridging group represented by the formula R^(a) ₂J′,where J′ is C or Si, and each R^(a) is, independently, C₁ to C₂₀substituted or unsubstituted hydrocarbyl, and the two R^(a) form acyclic structure incorporating J′ and the cyclic structure may be asaturated or partially saturated cyclic or fused ring system; and each Xis a univalent anionic ligand, or two Xs are joined and bound to themetal atom to form a metallocycle ring, or two Xs are joined to form achelating ligand, a diene ligand, or an alkylidene ligand; and (ii)obtaining a polymer having: 1) greater than 40% vinyl chain ends,relative to the total unsaturated chain ends, 2) a Tm of 70° C. or more;an Mw of 3000 to 300,000 g/mol, and 4) a g′_(vis) of 0.90 or less.

This invention also relates to a polymer having: 1) greater than 40%vinyl chain ends, relative to the total unsaturated chain ends(preferably at least X % vinyl chain ends (relative to totalunsaturations as measured by ¹H NMR, where X=47.8*g′_(vis)+45.1), 2) aTm of 70° C. or more; 3) an Mw of 3000 to 300,000 g/mol, and 4) ag′_(vis) of 0.90 or less.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is a graph of pressure of ethylene (psi) introduced into thereactor versus amount of vinyl termination in the polymer produced. Thelabels within the graph correspond to the examples number in Table 1.

DEFINITIONS

As used herein, the numbering scheme for the Periodic Table Groups isthe new notation as set out in CHEMICAL AND ENGINEERING NEWS, 63(5), 27(1985). Therefore, a “group 4 metal” is an element from group 4 of thePeriodic Table, e.g. Zr, Ti, and Hf

The terms “hydrocarbyl radical,” “hydrocarbyl” and “hydrocarbyl group”are used interchangeably throughout this document. Likewise the terms“group”, “radical”, and “substituent” are also used interchangeably inthis document. For purposes of this disclosure, “hydrocarbyl radical” isdefined to be a radical, which contains hydrogen atoms and up to 50carbon atoms and which may be linear, branched, or cyclic, and whencyclic, aromatic or non-aromatic.

Substituted hydrocarbyl radicals are radicals in which at least onehydrogen atom has been substituted with at least one functional groupsuch as NR*₂, OR*, SeR*, TeR*, PR*₂, AsR*₂, SbR*₂, SR*, BR*₂, SiR*₃,GeR*₃, SnR*₃, PbR*₃ and the like or where at least one non-hydrocarbonatom or group has been inserted within the hydrocarbyl radical, such as—O—, —S—, —Se—, —Te—, —N(R*)—, ═N—, —P(R*)—, ═P—, —As(R*)—, ═As—,—Sb(R*)—, ═Sb—, —B(R*)—, ═B—, —Si(R*)₂—, —Ge(R*)₂—, —Sn(R*)₂—, —Pb(R*)₂—and the like, where R* is independently a hydrocarbyl or halocarbylradical, and two or more R* may join together to form a substituted orunsubstituted saturated, partially unsaturated or aromatic cyclic orpolycyclic ring structure.

Halocarbyl radicals are radicals in which one or more hydrocarbylhydrogen atoms have been substituted with at least one halogen (e.g. F,Cl, Br, I) or halogen-containing group (e.g. CF₃).

Substituted halocarbyl radicals are radicals in which at least onehalocarbyl hydrogen or halogen atom has been substituted with at leastone functional group such as NR*₂, OR*, SeR*, TeR*, PR*₂, AsR*₂, SbR*₂,SR*, BR*₂, SiR*₃, GeR*₃, SnR*₃, PbR*₃ and the like or where at least onenon-carbon atom or group has been inserted within the halocarbyl radicalsuch as —O—, —S—, —Se—, —Te—, —N(R*)—, ═N—, —P(R*)—, ═P—, —As(R*)—,═As—, —Sb(R*)—, ═Sb—, —B(R*)—, ═B—, —Si(R*)₂—, —Ge(R*)₂—, —Sn(R*)₂—,—Pb(R*)₂— and the like, where R* is independently a hydrocarbyl orhalocarbyl radical provided that at least one halogen atom remains onthe original halocarbyl radical. Additionally, two or more R* may jointogether to form a substituted or unsubstituted saturated, partiallyunsaturated or aromatic cyclic or polycyclic ring structure.

In some embodiments of the invention, the hydrocarbyl radical isindependently selected from methyl, ethyl, ethenyl and isomers ofpropyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl,dodecyl, tridecyl, tetradecyl, pentadecyl, hexadecyl, heptadecyl,octadecyl, nonadecyl, eicosyl, heneicosyl, docosyl, tricosyl,tetracosyl, pentacosyl, hexacosyl, heptacosyl, octacosyl, nonacosyl,triacontyl, propenyl, butenyl, pentenyl, hexenyl, heptenyl, octenyl,nonenyl, decenyl, undecenyl, dodecenyl, tridecenyl, tetradecenyl,pentadecenyl, hexadecenyl, heptadecenyl, octadecenyl, nonadecenyl,eicosenyl, heneicosenyl, docosenyl, tricosenyl, tetracosenyl,pentacosenyl, hexacosenyl, heptacosenyl, octacosenyl, nonacosenyl,triacontenyl, propynyl, butynyl, pentynyl, hexynyl, heptynyl, octynyl,nonynyl, decynyl, undecynyl, dodecynyl, tridecynyl, tetradecynyl,pentadecynyl, hexadecynyl, heptadecynyl, octadecynyl, nonadecynyl,eicosynyl, heneicosynyl, docosynyl, tricosynyl, tetracosynyl,pentacosynyl, hexacosynyl, heptacosynyl, octacosynyl, nonacosynyl,triacontynyl, butadienyl, pentadienyl, hexadienyl, heptadienyl,octadienyl, nonadienyl, and decadienyl. Also included are isomers ofsaturated, partially unsaturated and aromatic cyclic and polycyclicstructures wherein the radical may additionally be subjected to thetypes of substitutions described above. Examples include phenyl,methylphenyl, dimethylphenyl, ethylphenyl, diethylphenyl, propylphenyl,dipropylphenyl, butylphenyl, dibutylphenyl, benzyl, methylbenzyl,naphthyl, anthracenyl, cyclopentyl, cyclopentenyl, cyclohexyl,cyclohexenyl, methylcyclohexyl, cycloheptyl, cycloheptenyl, norbornyl,norbornenyl, adamantyl and the like. For this disclosure, when a radicalis listed, it indicates that radical type and all other radicals formedwhen that radical type is subjected to the substitutions defined above.Alkyl, alkenyl and alkynyl radicals listed include all isomers includingcyclic isomers, for example, butyl includes n-butyl, 2-methylpropyl,1-methylpropyl, tent-butyl, and cyclobutyl (and analogous substitutedcyclopropyls); pentyl includes n-pentyl, cyclopentyl, 1-methylbutyl,2-methylbutyl, 3-methylbutyl, 1-ethylpropyl, and neopentyl (andanalogous substituted cyclobutyls and cyclopropyls); butenyl includes Eand Z forms of 1-butenyl, 2-butenyl, 3-butenyl, 1-methyl-1-propenyl,1-methyl-2-propenyl, 2-methyl-1-propenyl and 2-methyl-2-propenyl (andcyclobutenyls and cyclopropenyls). Cyclic compounds having substitutionsinclude all isomer forms, for example, methylphenyl would includeortho-methylphenyl, meta-methylphenyl and para-methylphenyl;dimethylphenyl would include 2,3-dimethylphenyl, 2,4-dimethylphenyl,2,5-dimethylphenyl, 2,6-diphenylmethyl, 3,4-dimethylphenyl, and3,5-dimethylphenyl.

For nomenclature purposes, the following numbering schemes are used forindenyl. It should be noted that indenyl can be considered acyclopentadienyl with fused a benzene ring. The structure below is drawnand named as an anion.

The following ring structures are substituted indenyls, where thesubstitution at the 5 and 6 positions forms a ring structure. Forspecific compound nomenclature purposes, these ligands are describedbelow. A similar numbering and nomenclature scheme is used for thesetypes of substituted indenyls that include indacenyls,cyclopenta[b]naphthalenyls, heterocyclopentanaphthyls,heterocyclopentaindenyls, and the like, as illustrated below. Eachstructure is drawn and named as an anion.

Non-limiting examples of indacenyls and cyclopenta[b]naphthalenylsinclude:

“Ring Structure” means atoms bonded together in one or more cyclicarrangements.

An “olefin,” alternatively referred to as “alkene,” is a linear,branched, or cyclic compound of carbon and hydrogen having at least onedouble bond. For purposes of this specification and the claims appendedthereto, when a polymer or copolymer is referred to as comprising anolefin, the olefin present in such polymer or copolymer is thepolymerized form of the olefin. For example, when a copolymer is said tohave an “ethylene” content of 35 wt % to 55 wt %, it is understood thatthe mer unit in the copolymer is derived from ethylene in thepolymerization reaction and said derived units are present at 35 wt % to55 wt %, based upon the weight of the copolymer. A “polymer” has two ormore of the same or different mer units. A “homopolymer” is a polymerhaving mer units that are the same. A “copolymer” is a polymer havingtwo or more mer units that are different from each other. A “terpolymer”is a polymer having three mer units that are different from each other.“Different” as used to refer to mer units indicates that the mer unitsdiffer from each other by at least one atom or are differentisomerically. Accordingly, the definition of copolymer, as used herein,includes terpolymers and the like. An oligomer is typically a polymerhaving a low molecular weight (such an Mn of less than 25,000 g/mol,preferably less than 2,500 g/mol) or a low number of mer units (such as75 mer units or less). An “ethylene polymer” or “ethylene copolymer” isa polymer or copolymer comprising at least 50 mole % ethylene derivedunits, a “propylene polymer” or “propylene copolymer” is a polymer orcopolymer comprising at least 50 mole % propylene derived units, and soon.

In the context of this document, “homopolymerization” would produce apolymer made from one type of monomer. For example, homopolymerizationof propylene would produce homopolypropylene; homopolymerization ofethylene would produce homopolyethylene; and the like. Likewise,“copolymerization” would produce polymers with more than one monomertype.

For the purposes of this invention, ethylene shall be considered anα-olefin.

An α-olefin may also include α-olefinic macromonomers of up to 2000 merunits.

The term “catalyst system” is defined to mean a catalystprecursor/activator pair, and optional co-activator, and an optionalsupport material. When “catalyst system” is used to describe such a pairbefore activation, it means the unactivated catalyst (precatalyst)together with an activator and, optionally, a co-activator. When it isused to describe such a pair after activation, it means the activatedcatalyst and the activator or other charge-balancing moiety. For thepurposes of this invention and the claims thereto, when catalyst systemsare described as comprising neutral stable forms of the components, itis well understood by one of ordinary skill in the art, that the ionicform of the component is the form that reacts with the monomers toproduce polymers.

A transition metal compound may be neutral as in a precatalyst, or acharged species with a counter ion as in an activated catalyst system.

Catalyst precursor is also often referred to as precatalyst, catalyst,catalyst compound, catalyst precursor, transition metal compound ortransition metal complex. These words are used interchangeably.Activator and cocatalyst are also used interchangeably. A scavenger is acompound that is typically added to facilitate oligomerization orpolymerization by scavenging impurities. Some scavengers may also act asactivators and may be referred to as co-activators. A co-activator, thatis not a scavenger, may also be used in conjunction with an activator inorder to form an active catalyst. In some embodiments a co-activator canbe pre-mixed with the transition metal compound to form an alkylatedtransition metal compound.

A polymerization catalyst system is a catalyst system that canpolymerize monomers to polymer. An “anionic ligand” is a negativelycharged ligand which donates one or more pairs of electrons to a metalion. A “neutral donor ligand” is a neutrally charged ligand whichdonates one or more pairs of electrons to a metal ion.

A metallocene catalyst is defined as an organometallic compound with atleast one π-bound cyclopentadienyl moiety (or substitutedcyclopentadienyl moiety such as indenyl) and more frequently two π-boundcyclopentadienyl moieties or substituted cyclopentadienyl moieties.

Noncoordinating anion (NCA) is defined to mean an anion either that doesnot coordinate to the catalyst metal cation or that does coordinate tothe metal cation, but only weakly. An NCA coordinates weakly enough thata neutral Lewis base, such as an olefinically or acetylenicallyunsaturated monomer can displace it from the catalyst center. Any metalor metalloid that can form a compatible, weakly coordinating complex maybe used or contained in the noncoordinating anion. Suitable metalsinclude, but are not limited to, aluminum, gold, and platinum. Suitablemetalloids include, but are not limited to, boron, aluminum, phosphorus,and silicon.

A stoichiometric activator can be either neutral or ionic. The termsionic activator, and stoichiometric ionic activator can be usedinterchangeably. Likewise, the terms neutral stoichiometric activator,and Lewis acid activator can be used interchangeably.

As used herein, Mn is number average molecular weight, Mw is weightaverage molecular weight, and Mz is z average molecular weight, wt % isweight percent, and mol % is mole percent. Molecular weight distribution(MWD), also referred to as polydispersity (PDI), is defined to be Mwdivided by Mn. Unless otherwise noted, all molecular weight units (e.g.,Mw, Mn, Mz) are g/mol. The following abbreviations may be used herein:Me is methyl, Et is ethyl, Pr is propyl, cPr is cyclopropyl, nPr isn-propyl, iPr is isopropyl, Bu is butyl, nBu is normal butyl, iBu isisobutyl, sBu is sec-butyl, tBu is tert-butyl, Oct is octyl, Ph isphenyl, Bn is benzyl, THF or thf is tetrahydrofuran, MAO ismethylalumoxane.

The term “continuous” means a system that operates without interruptionor cessation. For example a continuous process to produce a polymerwould be one where the reactants are continually introduced into one ormore reactors and polymer product is continually withdrawn.

For purposes of this invention, an “alkyl” group is a is a linear,branched, or cyclic radical of carbon and hydrogen. In a preferredembodiment, “alkyl” refers to linear alkyls.

Room temperature is 22° C., unless otherwise indicated.

DETAILED DESCRIPTION Catalyst Systems

Catalysts useful herein include catalysts capable of producing oligomerswith reactive polymerizable chain ends and capable of incorporatingoligomers with polymerizable chain ends to form branched oligomers orpolymers.

In the description herein, the catalyst may be described as a catalystprecursor, a pre-catalyst compound, a catalyst compound, or a transitionmetal compound, and these terms are used interchangeably. Apolymerization catalyst system is a catalyst system that can polymerizemonomers to polymer. A “catalyst system” is a combination of at leastone catalyst compound, at least one activator, an optional co-activator,and an optional support material. An “anionic ligand” is a negativelycharged ligand which donates one or more pairs of electrons to a metalion. A “neutral donor ligand” is a neutrally charged ligand whichdonates one or more pairs of electrons to a metal ion.

For the purposes of the embodiments and the claims thereto, whencatalyst systems are described as comprising neutral stable forms of thecomponents, it is well understood by one of ordinary skill in the art,that the ionic form of the component is the form that reacts with themonomers to produce polymers.

A metallocene catalyst is defined as an organometallic compound with atleast one π-bound cyclopentadienyl moiety (or substitutedcyclopentadienyl moiety) and more frequently two π-boundcyclopentadienyl-moieties or substituted moieties. This includes otherπ-bound moieties such as indenyls or fluorenyls or derivatives thereof.The term “substituted” means that a hydrogen group has been replacedwith a hydrocarbyl group, a heteroatom, or a heteroatom containinggroup. For example, methylcyclopentadiene (Cp) is a Cp group substitutedwith a methyl group.

The terms “hydrocarbyl radical,” “hydrocarbyl” and “hydrocarbyl group”are used interchangeably throughout this document. Likewise the terms“group”, “radical”, and “substituent” are also used interchangeably inthis document. For purposes of this disclosure, “hydrocarbyl radical” isdefined to be a radical, which contains hydrogen atoms and up to 50carbon atoms and which may be linear, branched, or cyclic, and whencyclic, aromatic or non-aromatic.

Substituted hydrocarbyl radicals are radicals in which at least onehydrogen atom has been substituted with at least one functional groupsuch as NR*₂, OR*, SeR*, TeR*, PR*₂, AsR*₂, SbR*₂, SR*, BR*₂, SiR*₃,GeR*₃, SnR*₃, PbR*₃ and the like or where at least one non-hydrocarbonatom or group has been inserted within the hydrocarbyl radical, such as—O—, —S—, —Se—, —Te—, —N(R*)—, ═N—, —P(R*)—, ═P—, —As(R*)—, ═As—,—Sb(R*)—, ═Sb—, —B(R*)—, ═B—, —Si(R*)₂—, —Ge(R*)₂—, —Sn(R*)₂—, —Pb(R*)₂—and the like, where R* is independently a hydrocarbyl or halocarbylradical, and two or more R* may join together to form a substituted orunsubstituted saturated, partially unsaturated or aromatic cyclic orpolycyclic ring structure.

Particularly useful metallocene catalysts include novel bridged ahafnium transition metal metallocene catalyst compounds having twoindenyl ligands substituted at the 4 positions with a C₁ to C₁₀ alkyl,where the 3 positions are hydrogen (assuming the bridge position iscounted as the one position) and the bridge is carbon or silicon whichis incorporated into a cyclic group comprising 3, 4, 5 or 6 siliconand/or carbon atoms that make up the cyclic ring, preferably the 2, 4positions, 4, 7 positions, 2, 4, 5 positions, 2, 4, 6 positions, 2, 4, 7positions, or 2, 4, 5, 6, 7 positions are substituted, preferably by aC₁ to C₁₀ alkyl group, and optionally, if alkyl substituted, the 4 and5, 5 and 6, and/or 6 and 7 positions may be bonded together to form aring structure.

In a preferred embodiment the metallocene catalyst compounds, andcatalyst systems comprising such compounds, are represented by theformula:

where each R³ is hydrogen; each R⁴ is independently a C₁-C₁₀ alkyl(preferably methyl, ethyl, propyl, butyl, pentyl, heptyl, hexyl, octyl,nonyl, decyl or an isomer thereof); each R², and R⁷ are independentlyhydrogen, or C₁-C₁₀ alkyl (preferably hydrogen, methyl, ethyl, propyl,butyl, pentyl, heptyl, hexyl, octyl, nonyl, decyl or an isomer thereof);each R⁵ and R⁶ are independently hydrogen, or C₁-C₅₀ substituted orunsubstituted hydrocarbyl (preferably hydrogen, methyl, ethyl, propyl,butyl, pentyl, heptyl, hexyl, octyl, nonyl, decyl or an isomer thereof);and R⁴ and R⁵, R⁵ and R⁶ and/or R⁶ and R⁷ may optionally be bondedtogether to form a ring structure; J is a bridging group represented bythe formula R^(a) ₂J, where J is C or Si, and each R^(a) is,independently C₁ to C₂₀ substituted or unsubstituted hydrocarbyl(preferably methyl, ethyl, propyl, butyl, pentyl, heptyl, hexyl, octyl,nonyl, decyl or an isomer thereof), and two R^(a) form a cyclicstructure incorporating J and the cyclic structure may be a saturated orpartially saturated cyclic or fused ring system; and each X is aunivalent anionic ligand, or two Xs are joined and bound to the metalatom to form a metallocycle ring, or two Xs are joined to form achelating ligand, a diene ligand, or an alkylidene ligand.

In a preferred embodiment of the invention, each R² is independently aC₁ to C₃ alkyl group, preferably methyl, ethyl, n-propyl, isopropyl orcyclopropyl, each R³, R⁵, R⁶, and R⁷ are hydrogen, and each R⁴ isindependently a C₁ to C₄ alkyl group, preferably methyl, ethyl,n-propyl, cyclopropyl, or n-butyl.

In a preferred embodiment of the invention, each R² is a C₁ to C₃ alkylgroup, preferably methyl, ethyl, n-propyl, isopropyl or cyclopropyl,each R³, R⁵, and R⁶ are hydrogen, and R⁴ and R⁷ are, independently, a C₁to C₄ alkyl group, preferably methyl, ethyl, propyl, butyl, or an isomerthereof.

In a preferred embodiment of the invention, each R², R⁴, and R⁷ areindependently methyl, ethyl, or n-propyl, each R⁵ and R⁶ areindependently, a C₁ to C₁₀ alkyl group, preferably methyl, ethyl,propyl, butyl, pentyl, heptyl, hexyl, octyl, nonyl, decyl or an isomerthereof, R³ is hydrogen, and R⁵ and R⁶ are joined together to form a5-membered partially unsaturated ring.

In a preferred embodiment of the invention, each R², R⁴ and R⁷ are thesame and are selected from the group consisting of C₁ to C₃ alkyl group,preferably methyl, ethyl, propyl, and isomers thereof, and R³, R⁵ and R⁶are hydrogen.

In a preferred embodiment of the invention, J is preferably representedby the formula:

wherein J′ is a carbon or silicon atom, x is 1, 2, 3, or 4, preferably 2or 3, and each R′ is, independently, hydrogen or C₁-C₁₀ hydrocarbyl,preferably hydrogen. Particularly preferred J groups includecyclopentamethylenesilylene, cyclotetramethylenesilylene,cyclotrimethylenesilylene, and the like.

In a preferred embodiment of the invention, each X is, independently,selected from the group consisting of hydrocarbyl radicals having from 1to 20 carbon atoms, hydrides, amides, alkoxides, sulfides, phosphides,halides, dienes, amines, phosphines, ethers, and a combination thereof,(two X′s may form a part of a fused ring or a ring system), preferablyeach X is independently selected from halides and C₁ to C₅ alkyl groups,preferably each X is a methyl, ethyl, propyl, butyl or pentyl group,preferably a methyl group.

In a preferred embodiment of the invention, R⁴ is not an aryl group(substituted or unsubstituted). An aryl group is defined to be a singleor multiple fused ring group where at least on ring is aromatic. Asubstituted aryl group is an aryl group where a hydrogen has beenreplaced by a heteroatom or heteroatom containing group. Examples ofaryl groups include phenyl, benzyl, carbazolyl, naphthyl, and the like.

In a preferred embodiment this invention, R², R⁴ and R⁷ are not asubstituted or unsubstituted aryl group.

In a preferred embodiment this invention, R², R⁴, R⁵, R⁶ and R⁷ are nota substituted or unsubstituted aryl group.

Metallocene compounds that are particularly useful in this inventioninclude one or more of:

-   cyclotetramethylenesilylene-bis(2,4,7-trimethylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2,4,7-trimethylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2,4,7-trimethylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(2,4-dimethylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2,4-dimethylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2,4-dimethylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(4,7-dimethylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(4,7-dimethylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(4,7-dimethylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(2-methyl-4-cyclopropylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2-methyl-4-cyclopropylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2-methyl-4-cyclopropylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(2-ethyl-4-cyclopropylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2-ethyl-4-cyclopropylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2-ethyl-4-cyclopropylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(2-methyl-4-t-butylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2-methyl-4-t-butylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2-methyl-4-t-butylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(4,7-diethylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(4,7-diethylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(4,7-diethylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(2,4-diethylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2,4-diethylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2,4-diethylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(2-methyl-4,7-diethylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2-methyl-4,7-diethylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2-methyl-4,7-diethylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(2-ethyl-4-methylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2-ethyl-4-methylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2-ethyl-4-methylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(2-methyl-4-isopropylinden-1-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(2-methyl-4-isopropylinden-1-yl)hafnium    dimethyl,-   cyclotrimethylenesilylene-bis(2-methyl-4-isopropylinden-1-yl)hafnium    dimethyl,-   cyclotetramethylenesilylene-bis(4,6,8-trimethyl-1,2,3-trihydro-s-indacen-5-yl)hafnium    dimethyl,-   cyclopentamethylenesilylene-bis(4,6,8-trimethyl-1,2,3-trihydro-s-indacen-5-yl)hafnium    dimethyl, and-   cyclotrimethylenesilylene-bis(4,6,8-trimethyl-1,2,3-trihydro-s-indacen-5-yl)hafnium    dimethyl.

In a preferred embodiment of the invention, the catalyst compound is inthe rac form. In a preferred embodiment of the invention, at least 90 wt% of the catalyst compound is in the rac form, based upon the weight ofthe rac and meso forms present, preferably from 92 to 100 wt %,preferably from 95 to 100 wt %, preferably from 98 to 100 wt %. In apreferred embodiment of the invention, the catalyst compound is greaterthan 90% rac, preferably greater than 95% rac, preferably greater than98% rac.

In a preferred embodiment, the hafnium bis-indenyl metallocene compoundused herein is at least 90% rac isomer and is the indenyl groups aresubstituted at the 4 position with a C₁ to C₁₀ alkyl group, the 3position is hydrogen, the bridge is carbon or silicon which isincorporated into a 4, 5 or 6 membered ring.

The metallocene compounds described herein are synthesized according toprocedures describe in U.S. Ser. No. 61/847,442, filed Jul. 17, 2013.

Activators

The terms “cocatalyst” and “activator” are used herein interchangeablyand are defined to be any compound which can activate any one of thecatalyst compounds described above by converting the neutral catalystcompound to a catalytically active catalyst compound cation.Non-limiting activators, for example, include alumoxanes, aluminumalkyls, ionizing activators, which may be neutral or ionic, andconventional-type cocatalysts. Preferred activators typically includealumoxane compounds, modified alumoxane compounds, and ionizing anionprecursor compounds that abstract a reactive, a-bound, metal ligandmaking the metal complex cationic and providing a charge-balancingnoncoordinating or weakly coordinating anion.

In one embodiment, alumoxane activators are utilized as an activator inthe catalyst composition. Alumoxanes are generally oligomeric compoundscontaining —Al(R¹)—O-sub-units, where R¹ is an alkyl group. Examples ofalumoxanes include methylalumoxane (MAO), modified methylalumoxane(MMAO), ethylalumoxane and isobutylalumoxane. Alkylalumoxanes andmodified alkylalumoxanes are suitable as catalyst activators,particularly when the abstractable ligand is an alkyl, halide, alkoxideor amide. Mixtures of different alumoxanes and modified alumoxanes mayalso be used. It may be preferable to use a visually clearmethylalumoxane. A cloudy or gelled alumoxane can be filtered to producea clear solution or clear alumoxane can be decanted from the cloudysolution. A useful alumoxane is a modified methyl alumoxane (MMAO)cocatalyst type 3A (commercially available from Akzo Chemicals, Inc.under the trade name Modified Methylalumoxane type 3A, covered underpatent number U.S. Pat. No. 5,041,584).

When the activator is an alumoxane (modified or unmodified), someembodiments select the maximum amount of activator at a 5000-fold molarexcess Al/M over the catalyst compound (per metal catalytic site). Theminimum activator-to-catalyst-compound is a 1:1 molar ratio. Alternatepreferred ranges include from 1:1 to 500:1, alternately from 1:1 to200:1, alternately from 1:1 to 100:1, or alternately from 1:1 to 50:1.

In an alternate embodiment, little or no alumoxane is used in thepolymerization processes described herein. Preferably, alumoxane ispresent at zero mole %, alternately the alumoxane is present at a molarratio of aluminum to catalyst compound transition metal less than 500:1,preferably less than 300:1, preferably less than 100:1, preferably lessthan 1:1.

The term “non-coordinating anion” (NCA) means an anion which either doesnot coordinate to a cation or which is only weakly coordinated to acation thereby remaining sufficiently labile to be displaced by aneutral Lewis base. “Compatible” non-coordinating anions are those whichare not degraded to neutrality when the initially formed complexdecomposes. Further, the anion will not transfer an anionic substituentor fragment to the cation so as to cause it to form a neutral transitionmetal compound and a neutral by-product from the anion. Non-coordinatinganions useful in accordance with this invention are those that arecompatible, stabilize the transition metal cation in the sense ofbalancing its ionic charge at +1, and yet retain sufficient lability topermit displacement during polymerization.

It is within the scope of this invention to use an ionizing orstoichiometric activator, neutral or ionic, such as tri (n-butyl)ammonium tetrakis (pentafluorophenyl) borate, a tris perfluorophenylboron metalloid precursor or a tris perfluoronaphthyl boron metalloidprecursor, polyhalogenated heteroborane anions (WO 98/43983), boric acid(U.S. Pat. No. 5,942,459), or combination thereof. It is also within thescope of this invention to use neutral or ionic activators alone or incombination with alumoxane or modified alumoxane activators.

Examples of neutral stoichiometric activators include tri-substitutedboron, tellurium, aluminum, gallium, and indium, or mixtures thereof Thethree substituent groups are each independently selected from alkyls,alkenyls, halogens, substituted alkyls, aryls, arylhalides, alkoxy, andhalides. Preferably, the three groups are independently selected fromhalogen, mono or multicyclic (including halosubstituted) aryls, alkyls,and alkenyl compounds, and mixtures thereof, preferred are alkenylgroups having 1 to 20 carbon atoms, alkyl groups having 1 to 20 carbonatoms, alkoxy groups having 1 to 20 carbon atoms and aryl groups having3 to 20 carbon atoms (including substituted aryls). More preferably, thethree groups are alkyls having 1 to 4 carbon groups, phenyl, naphthyl,or mixtures thereof. Even more preferably, the three groups arehalogenated, preferably fluorinated, aryl groups. A preferred neutralstoichiometric activator is tris perfluorophenyl boron or trisperfluoronaphthyl boron.

Ionic stoichiometric activator compounds may contain an active proton,or some other cation associated with, but not coordinated to, or onlyloosely coordinated to, the remaining ion of the ionizing compound. Suchcompounds and the like are described in European publications EP 0 570982 A; EP 0 520 732 A; EP 0 495 375 A; EP 0 500 944 B1; EP 0 277 003 A;EP 0 277 004 A; U.S. Pat. Nos. 5,153,157; 5,198,401; 5,066,741;5,206,197; 5,241,025; 5,384,299; 5,502,124; and U.S. patent applicationSer. No. 08/285,380, filed Aug. 3, 1994; all of which are herein fullyincorporated by reference.

Preferred compounds useful as an activator in the process of thisinvention comprise a cation, which is preferably a Bronsted acid capableof donating a proton, and a compatible non-coordinating anion whichanion is relatively large (bulky), capable of stabilizing the activecatalyst species (the Group 4 cation) which is formed when the twocompounds are combined and said anion will be sufficiently labile to bedisplaced by olefinic, diolefinic and acetylenically unsaturatedsubstrates or other neutral Lewis bases, such as ethers, amines, and thelike. Two classes of useful compatible non-coordinating anions have beendisclosed in EP 0 277,003 A1, and EP 0 277,004 A1: 1) anioniccoordination complexes comprising a plurality of lipophilic radicalscovalently coordinated to and shielding a central charge-bearing metalor metalloid core; and 2) anions comprising a plurality of boron atomssuch as carboranes, metallacarboranes, and boranes.

In a preferred embodiment, the stoichiometric activators include acation and an anion component, and are preferably represented by thefollowing formula (1):

(Z)_(d) ⁺(Ad⁻)   (1)

wherein Z is (L-H) or a reducible Lewis Acid, L is an neutral Lewisbase; H is hydrogen; (L-H)⁺ is a Bronsted acid; A^(d−) is anon-coordinating anion having the charge d−; and d is an integer from 1to 3.

When Z is (L-H) such that the cation component is (L-H)_(d) ⁺, thecation component may include Bronsted acids such as protonated Lewisbases capable of protonating a moiety, such as an alkyl or aryl, fromthe bulky ligand metallocene containing transition metal catalystprecursor, resulting in a cationic transition metal species. Preferably,the activating cation (L-H)_(d) ⁺ is a Bronsted acid, capable ofdonating a proton to the transition metal catalytic precursor resultingin a transition metal cation, including ammoniums, oxoniums,phosphoniums, silyliums, and mixtures thereof, preferably ammoniums ofmethylamine, aniline, dimethylamine, diethylamine, N-methylaniline,diphenylamine, trimethylamine, triethylamine, N,N-dimethylaniline,methyldiphenylamine, pyridine, p-bromo N,N-dimethylaniline,p-nitro-N,N-dimethylaniline, phosphoniums from triethylphosphine,triphenylphosphine, and diphenylphosphine, oxoniums from ethers, such asdimethyl ether diethyl ether, tetrahydrofuran, and dioxane, sulfoniumsfrom thioethers, such as diethyl thioethers and tetrahydrothiophene, andmixtures thereof

When Z is a reducible Lewis acid it is preferably represented by theformula: (Ar₃C⁺), where Ar is aryl or aryl substituted with aheteroatom, a C₁ to C₄₀ hydrocarbyl, or a substituted C₁ to C₄₀hydrocarbyl, preferably the reducible Lewis acid is represented by theformula: (Ph₃C⁺), where Ph is phenyl or phenyl substituted with aheteroatom, a C₁ to C₄₀ hydrocarbyl, or a substituted C₁ to C₄₀hydrocarbyl. In a preferred embodiment, the reducible Lewis acid istriphenyl carbenium.

The anion component A^(d−) include those having the formula[Mk+Q_(n)]^(d−) wherein k is 1, 2, or 3; n is 1, 2, 3, 4, 5, or 6,preferably 3, 4, 5 or 6; n−k=d; M is an element selected from Group 13of the Periodic Table of the Elements, preferably boron or aluminum, andQ is independently a hydride, bridged or unbridged dialkylamido, halide,alkoxide, aryloxide, hydrocarbyl, substituted hydrocarbyl, halocarbyl,substituted halocarbyl, and halosubstituted-hydrocarbyl radicals, said Qhaving up to 20 carbon atoms with the proviso that in not more than oneoccurrence is Q a halide, and two Q groups may form a ring structure.Preferably, each Q is a fluorinated hydrocarbyl group having 1 to 20carbon atoms, more preferably each Q is a fluorinated aryl group, andmost preferably each Q is a pentafluoro aryl group. Examples of suitableA^(d−) components also include diboron compounds as disclosed in U.S.Pat. No. 5,447,895, which is fully incorporated herein by reference.

In a preferred embodiment, this invention relates to a method topolymerize olefins comprising contacting olefins (preferably ethylene)with metallocene catalyst compound described herein, a chain transferagent and a boron containing NCA activator represented by the formula(2):

Z_(d) ⁺(A^(d−))   (2)

where: Z is (L-H) or a reducible Lewis acid; L is an neutral Lewis base(as further described above); H is hydrogen; (L-H) is a Bronsted acid(as further described above); A^(d−) is a boron containingnon-coordinating anion having the charge d (as further described above);d is 1, 2, or 3.

In a preferred embodiment in any NCA's represented by Formula 2described above, the reducible Lewis acid is represented by the formula:(Ar₃C⁺), where Ar is aryl or aryl substituted with a heteroatom, a C₁ toC₄₀ hydrocarbyl, or a substituted C1 to C40 hydrocarbyl, preferably thereducible Lewis acid is represented by the formula: (Ph₃C⁺), where Ph isphenyl or phenyl substituted with a heteroatom, a C₁ to C₄₀ hydrocarbyl,or a substituted C₁ to C₄₀ hydrocarbyl.

In a preferred embodiment in any of the NCA's represented by Formula 2described above, Z_(d) ⁺ is represented by the formula: (L-H)_(d)+,wherein L is an neutral Lewis base; H is hydrogen; (L-H) is a Bronstedacid; and d is 1, 2, or 3, preferably (L-H)_(d) ⁺ is a Bronsted acidselected from ammoniums, oxoniums, phosphoniums, silyliums, and mixturesthereof.

In a preferred embodiment in any of the NCA's represented by Formula 2described above, the anion component A^(d−) is represented by theformula [M^(*k*+)Q*_(n)*]^(d*−) wherein k* is 1, 2, or 3; n* is 1, 2, 3,4, 5, or 6 (preferably 1, 2, 3, or 4); n*−k*=d*; M* is boron; and Q* isindependently selected from hydride, bridged or unbridged dialkylamido,halide, alkoxide, aryloxide, hydrocarbyl, substituted hydrocarbyl,halocarbyl, substituted halocarbyl, and halosubstituted-hydrocarbylradicals, said Q* having up to 20 carbon atoms with the proviso that innot more than 1 occurrence is Q* a halide.

This invention also relates to a method to polymerize olefins comprisingcontacting olefins (such as ethylene) with an metallocene catalystcompound described herein, a chain transfer agent and an NCA activatorrepresented by the formula (3):

R_(n)M**(ArNHal)_(4-n)   (3)

where R is a monoanionic ligand; M** is a Group 13 metal or metalloid;ArNHal is a halogenated, nitrogen-containing aromatic ring, polycyclicaromatic ring, or aromatic ring assembly in which two or more rings (orfused ring systems) are joined directly to one another or together; andn is 0, 1, 2, or 3. Typically the NCA comprising an anion of Formula 3also comprises a suitable cation that is essentially non-interferingwith the ionic catalyst complexes formed with the transition metalcompounds, preferably the cation is Z_(d) ⁺ as described above.

In a preferred embodiment in any of the NCA's comprising an anionrepresented by Formula 3 described above, R is selected from the groupconsisting of substituted or unsubstituted C₁ to C₃₀ hydrocarbylaliphatic or aromatic groups, where substituted means that at least onehydrogen on a carbon atom is replaced with a hydrocarbyl, halide,halocarbyl, hydrocarbyl or halocarbyl substituted organometalloid,dialkylamido, alkoxy, aryloxy, alkysulfido, arylsulfido, alkylphosphido,arylphosphide, or other anionic substituent; fluoride; bulky alkoxides,where bulky means C₄ to C₂₀ hydrocarbyl groups; —SR¹, —NR² ₂, and —PR³₂, where each R¹, R², or R³ is independently a substituted orunsubstituted hydrocarbyl as defined above; or a C₁ to C₃₀ hydrocarbylsubstituted organometalloid.

In a preferred embodiment in any of the NCA's comprising an anionrepresented by Formula 3 described above, the NCA also comprises cationcomprising a reducible Lewis acid represented by the formula: (Ar₃C⁺),where Ar is aryl or aryl substituted with a heteroatom, a C₁ to C₄₀hydrocarbyl, or a substituted C₁ to C₄₀ hydrocarbyl, preferably thereducible Lewis acid represented by the formula: (Ph₃C+), where Ph isphenyl or phenyl substituted with a heteroatom, a C₁ to C₄₀ hydrocarbyl,or a substituted C₁ to C₄₀ hydrocarbyl.

In a preferred embodiment in any of the NCA's comprising an anionrepresented by Formula 3 described above, the NCA also comprises acation represented by the formula, (L-H)_(d) ⁺, wherein L is an neutralLewis base; H is hydrogen; (L-H) is a Bronsted acid; and d is 1, 2, or3, preferably (L-H)_(d) ⁺ is a Bronsted acid selected from ammoniums,oxoniums, phosphoniums, silyliums, and mixtures thereof.

Further examples of useful activators include those disclosed in U.S.Pat. Nos. 7,297,653 and 7,799,879.

Another activator useful herein comprises a salt of a cationic oxidizingagent and a noncoordinating, compatible anion represented by the formula(4):

(OX^(e+))_(d)(A^(d−))_(e)   (4)

wherein OX^(e+) is a cationic oxidizing agent having a charge of e+; eis 1, 2, or 3; d is 1, 2 or 3;

-   -   and A^(d−) is a non-coordinating anion having the charge of d−        (as further described above).

Examples of cationic oxidizing agents include: ferrocenium,hydrocarbyl-substituted ferrocenium, Ag⁺, or Pb⁺². Preferred embodimentsof A^(d−) include tetrakis(pentafluorophenyl)borate.

In another embodiment, metallocene catalyst compounds described hereincan be used with Bulky activators. A “Bulky activator” as used hereinrefers to anionic activators represented by the formula:

where:each R₁ is, independently, a halide, preferably a fluoride;

-   -   each R₂ is, independently, a halide, a C₆ to C₂₀ substituted        aromatic hydrocarbyl group or a siloxy group of the formula        —O—Si—R_(a), where R_(a) is a C₁ to C₂₀ hydrocarbyl or        hydrocarbylsilyl group (preferably R₂ is a fluoride or a        perfluorinated phenyl group);    -   each R₃ is a halide, C₆ to C₂₀ substituted aromatic hydrocarbyl        group or a siloxy group of the formula —O—Si—R_(a), where R_(a)        is a C₁ to C₂₀ hydrocarbyl or hydrocarbylsilyl group (preferably        R₃ is a fluoride or a C₆ perfluorinated aromatic hydrocarbyl        group); wherein R₂ and R₃ can form one or more saturated or        unsaturated, substituted or unsubstituted rings (preferably R₂        and R₃ form a perfluorinated phenyl ring);    -   L is an neutral Lewis base; (L-H)⁺ is a Bronsted acid; d is 1,        2, or 3;    -   wherein the anion has a molecular weight of greater than 1020        g/mol; and    -   wherein at least three of the substituents on the B atom each        have a molecular volume of greater than 250 cubic A, alternately        greater than 300 cubic A, or alternately greater than 500 cubic        A.

“Molecular volume” is used herein as an approximation of spatial stericbulk of an activator molecule in solution. Comparison of substituentswith differing molecular volumes allows the substituent with the smallermolecular volume to be considered “less bulky” in comparison to thesubstituent with the larger molecular volume. Conversely, a substituentwith a larger molecular volume may be considered “more bulky” than asubstituent with a smaller molecular volume.

Molecular volume may be calculated as reported in “A Simple “Back of theEnvelope” Method for Estimating the Densities and Molecular Volumes ofLiquids and Solids,” Journal of Chemical Education, Vol. 71, No. 11,November 1994, pp. 962-964. Molecular volume (MV), in units of cubic Å,is calculated using the formula: MV=8.3V_(s), where V_(s) is the scaledvolume. V_(s) is the sum of the relative volumes of the constituentatoms, and is calculated from the molecular formula of the substituentusing the following table of relative volumes. For fused rings, theV_(s) is decreased by 7.5% per fused ring.

Element Relative Volume H 1 1^(st) short period, Li to F 2 2^(nd) shortperiod, Na to Cl 4 1^(st) long period, K to Br 5 2^(nd) long period, Rbto I 7.5 3^(rd) long period, Cs to Bi 9

Exemplary bulky substituents of activators suitable herein and theirrespective scaled volumes and molecular volumes are shown in the tablebelow. The dashed bonds indicate binding to boron, as in the generalformula above.

MV Molecular Formula of Per subst. Total MV Activator Structure of boronsubstituents each substituent (Å³) (Å³) Dimethylaniliniumtetrakis(perfluoronaphthyl)borate

C₁₀F₇ 261 1044 Dimethylanilinium tetrakis(perfluorobiphenyl)borate

C₁₂F₉ 349 1396 [4-tButyl-PhNMe₂H] [(C₆F₃(C₆F₅)₂)₄B]

C₁₈F₁₃ 515 2060

Exemplary bulky activators useful in catalyst systems herein include:trimethylammonium tetrakis(perfluoronaphthyl)borate, triethylammoniumtetrakis(perfluoronaphthyl)borate, tripropylammoniumtetrakis(perfluoronaphthyl)borate, tri(n-butyl)ammoniumtetrakis(perfluoronaphthyl)borate, tri(t-butyl)ammoniumtetrakis(perfluoronaphthyl)borate, N,N-dimethylaniliniumtetrakis(perfluoronaphthyl)borate, N,N-diethylaniliniumtetrakis(perfluoronaphthyl)borate,N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(perfluoronaphthyl)borate, tropilliumtetrakis(perfluoronaphthyl)borate, triphenylcarbeniumtetrakis(perfluoronaphthyl)borate, triphenylphosphoniumtetrakis(perfluoronaphthyl)borate, triethylsilyliumtetrakis(perfluoronaphthyl)borate, benzene(diazonium)tetrakis(perfluoronaphthyl)borate, trimethylammoniumtetrakis(perfluorobiphenyl)borate, triethylammoniumtetrakis(perfluorobiphenyl)borate, tripropylammoniumtetrakis(perfluorobiphenyl)borate, tri(n-butyl)ammoniumtetrakis(perfluorobiphenyl)borate, tri(t-butyl)ammoniumtetrakis(perfluorobiphenyl)borate, N,N-dimethylaniliniumtetrakis(perfluorobiphenyl)borate, N,N-diethylaniliniumtetrakis(perfluorobiphenyl)borate,N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(perfluorobiphenyl)borate, tropilliumtetrakis(perfluorobiphenyl)borate, triphenylcarbeniumtetrakis(perfluorobiphenyl)borate, triphenylphosphoniumtetrakis(perfluorobiphenyl)borate, triethylsilyliumtetrakis(perfluorobiphenyl)borate, benzene(diazonium)tetrakis(perfluorobiphenyl)borate, [4-t-butyl-PhNMe₂H][(C₆F₃(C₆F₅)₂)₄B],and the types disclosed in U.S. Pat. No. 7,297,653.

Illustrative, but not limiting, examples of boron compounds which may beused as an activator in the processes of this invention are:

-   trimethylammonium tetraphenylborate, triethylammonium    tetraphenylborate, tripropylammonium tetraphenylborate,    tri(n-butyl)ammonium tetraphenylborate, tri(t-butyl)ammonium    tetraphenylborate, N,N-dimethylanilinium tetraphenylborate,    N,N-diethylanilinium tetraphenylborate,    N,N-dimethyl-(2,4,6-trimethylanilinium) tetraphenylborate,    tropillium tetraphenylborate, triphenylcarbenium tetraphenylborate,    triphenylphosphonium tetraphenylborate triethylsilylium    tetraphenylborate, benzene(diazonium)tetraphenylborate,    trimethylammonium tetrakis(pentafluorophenyl)borate,    triethylammonium tetrakis(pentafluorophenyl)borate,    tripropylammonium tetrakis(pentafluorophenyl)borate,    tri(n-butyl)ammonium tetrakis(pentafluorophenyl)borate,    tri(sec-butyl)ammonium tetrakis(pentafluorophenyl)borate,    N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate,    N,N-diethylanilinium tetrakis(pentafluorophenyl)borate,    N,N-dimethyl-(2,4,6-trimethylanilinium)    tetrakis(pentafluorophenyl)borate, tropillium to    tetrakis(pentafluorophenyl)borate, triphenylcarbenium    tetrakis(pentafluorophenyl)borate, triphenylphosphonium    tetrakis(pentafluorophenyl)borate, triethylsilylium    tetrakis(pentafluorophenyl)borate,    benzene(diazonium)tetrakis(pentafluorophenyl)borate,    trimethylammonium tetrakis-(2,3,4,6-tetrafluorophenyl) borate,    triethylammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate,    tripropylammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate,    tri(n-butyl) ammonium tetrakis-(2,3,4,6-tetrafluoro-phenyl)borate,    dimethyl(t-butyl)ammonium    tetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-dimethylanilinium    tetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-diethylanilinium    tetrakis-(2,3,4,6-tetrafluorophenyl)borate,    N,N-dimethyl-(2,4,6-trimethylanilinium)    tetrakis-(2,3,4,6-tetrafluorophenyl)borate, tropillium    tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylcarbenium    tetrakis-(2,3,4,6-tetrailuorophenyl)borate, triphenylphosphonium    tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triethylsilylium    tetrakis-(2,3,4,6-tetrafluorophenyl)borate,    benzene(diazonium)tetrakis-(2,3,4,6-tetrafluorophenyl)borate,    trimethylammonium tetrakis(perfluoronaphthyl)borate,    triethylammonium tetrakis(perfluoronaphthyl)borate,    tripropylammonium tetrakis(perfluoronaphthyl)borate,    tri(n-butyl)ammonium tetrakis(perfluoronaphthyl)borate,    tri(t-butyl)ammonium tetrakis(perfluoronaphthyl)borate,    N,N-dimethylanilinium tetrakis(perfluoronaphthyl)borate,    N,N-diethylanilinium tetrakis(perfluoronaphthyl)borate,    N,N-dimethyl-(2,4,6-trimethylanilinium)    tetrakis(perfluoronaphthyl)borate, tropillium    tetrakis(perfluoronaphthyl)borate, triphenylcarbenium    tetrakis(perfluoronaphthyl)borate, triphenylphosphonium    tetrakis(perfluoronaphthyl)borate, triethylsilylium    tetrakis(perfluoronaphthyl)borate, benzene(diazonium)    tetrakis(perfluoronaphthyl)borate, trimethylammonium    tetrakis(perfluorobiphenyl)borate, triethyl ammonium    tetrakis(perfluorobiphenyl)borate, tripropylammonium    tetrakis(perfluorobiphenyl)borate, tri(n-butyl)ammonium    tetrakis(perfluorobiphenyl)borate, tri(t-butyl)ammonium    tetrakis(perfluorobiphenyl)borate, N,N-dimethylanilinium    tetrakis(perfluorobiphenyl)b orate, N,N-diethylanilinium    tetrakis(perfluorobiphenyl)borate,    N,N-dimethyl-(2,4,6-trimethylanilinium)    tetrakis(perfluorobiphenyl)borate, tropillium    tetrakis(perfluorobiphenyl)borate, triphenylcarbenium    tetrakis(perfluorobipheny orate, triphenylphosphonium    tetrakis(perfluorobiphenyl)borate, triethylsilylium    tetrakis(perfluorobiphenyl)borate, benzene(diazonium)    tetrakis(perfluorobiphenyl)borate, trimethylammonium    tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triethylammonium    tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tripropylammonium    tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tri(n-butyl)ammonium    tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tri(t-butyl)ammonium    tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,    N,N-dimethylanilinium    tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-diethylanilinium    tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,    N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,    tropillium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,    triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,    triphenylphosphonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,    triethylsilylium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,    benzene(diazonium) tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,    and dialkyl ammonium salts, such as: di-(i-propyl)ammonium    tetrakis(pentafluorophenyl)borate, and dicyclohexylammonium    tetrakis(pentafluorophenyl)borate; and additional tri-substituted    phosphonium salts, such as tri(o-tolyl)phosphonium    tetrakis(pentafluorophenyl)borate, and    tri(2,6-dimethylphenyl)phosphonium    tetrakis(pentafluorophenyl)borate.

Preferred activators include N,N-dimethylaniliniumtetrakis(perfluoronaphthyl)borate, N,N-dimethylaniliniumtetrakis(perfluorobiphenyl)borate, N,N-dimethylaniliniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbeniumtetrakis(perfluoronaphthyl)borate, triphenylcarbeniumtetrakis(perfluorobiphenyl)borate, triphenylcarbeniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbeniumtetrakis(perfluorophenyl)borate, [Ph₃C⁺][B(C₆F₅)₄ ⁻], [Me₃NH⁺][B(C₆F₅)₄⁻];1-(4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluorophenyl)pyrrolidinium;and tetrakis(pentafluorophenyl)borate,4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluoropyridine.

In a preferred embodiment, the activator comprises a triaryl carbonium(such as triphenylcarbenium tetraphenylborate, triphenylcarbeniumtetrakis(pentafluorophenyl)borate, triphenylcarbeniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylcarbeniumtetrakis(perfluoronaphthyl)borate, triphenylcarbeniumtetrakis(perfluorobiphenyl)borate, triphenylcarbeniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate).

In another embodiment, the activator comprises one or more oftrialkylammonium tetrakis(pentafluorophenyl)borate, N,N-dialkylaniliniumtetrakis(pentafluorophenyl)borate,N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(pentafluorophenyl)borate, trialkylammoniumtetrakis-(2,3,4,6-tetrafluorophenyl) borate, N,N-dialkylaniliniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, trialkylammoniumtetrakis(perfluoronaphthyl)borate, N,N-dialkylaniliniumtetrakis(perfluoronaphthyl)borate, trialkylammoniumtetrakis(perfluorobiphenyl)borate, N,N-dialkylaniliniumtetrakis(perfluorobiphenyl)borate, trialkylammoniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-dialkylaniliniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate,N,N-dialkyl-(2,4,6-trimethylanilinium)tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, di-(i-propyl)ammoniumtetrakis(pentafluorophenyl)borate, (where alkyl is methyl, ethyl,propyl, n-butyl, sec-butyl, or t-butyl).

In a particularly preferred embodiment, the activator used incombination with any catalyst compound(s) described herein isN,N-dimethylanilinium tetrakis (perfluoronaphthyl)borate.

In a preferred embodiment, any of the activators described herein may bemixed together before or after combination with the catalyst compound,preferably before being mixed with the catalyst compound.

In some embodiments two NCA activators may be used in the polymerizationand the molar ratio of the first NCA activator to the second NCAactivator can be any ratio. In some embodiments, the molar ratio of thefirst NCA activator to the second NCA activator is 0.01:1 to 10,000:1,preferably 0.1:1 to 1000:1, preferably 1:1 to 100:1.

Further, the typical activator-to-catalyst ratio, e.g., all NCAactivators-to-catalyst ratio is a 1:1 molar ratio. Alternate preferredranges include from 0.1:1 to 100:1, alternately from 0.5:1 to 200:1,alternately from 1:1 to 500:1 alternately from 1:1 to 1000:1. Aparticularly useful range is from 0.5:1 to 10:1, preferably 1:1 to 5:1.

It is also within the scope of this invention that the catalystcompounds can be combined with combinations of alumoxanes and NCA's (seefor example, U.S. Pat. No. 5,153,157, U.S. Pat. No. 5,453,410, EP 0 573120 B1, WO 94/07928, and WO 95/14044 which discuss the use of analumoxane in combination with an ionizing activator).

Optional Scavengers or Co-Activators

In addition to the activator compounds, scavengers or co-activators maybe used. Aluminum alkyl or organoaluminum compounds which may beutilized as scavengers or co-activators include, for example,trimethylaluminum, triethylaluminum, triisobutylaluminum,tri-n-hexylaluminum, tri-n-octylaluminum and the like. Other oxophilicspecies such as diethyl zinc may be used.

Optional Support Materials

In embodiments herein, the catalyst system may comprise an inert supportmaterial. Preferably the supported material is a porous supportmaterial, for example, talc, and inorganic oxides. Other supportmaterials include zeolites, clays, organoclays, or any other organic orinorganic support material and the like, or mixtures thereof.

Preferably, the support material is an inorganic oxide in a finelydivided form. Suitable inorganic oxide materials for use in metallocenecatalyst systems herein include Groups 2, 4, 13, and 14 metal oxides,such as silica, alumina, and mixtures thereof. Other inorganic oxidesthat may be employed either alone or in combination with the silica, oralumina are magnesia, titania, zirconia, and the like. Other suitablesupport materials, however, can be employed, for example, finely dividedfunctionalized polyolefins, such as finely divided polyethylene.Particularly useful supports include magnesia, titania, zirconia,montmorillonite, phyllosilicate, zeolites, talc, clays, and the like.Also, combinations of these support materials may be used, for example,silica-chromium, silica-alumina, silica-titania, and the like. Preferredsupport materials include Al₂O₃, ZrO₂, SiO₂, and combinations thereof,more preferably SiO₂, Al₂O₃, or SiO₂/Al₂O₃.

It is preferred that the support material, most preferably an inorganicoxide, has a surface area in the range of from about 10 to about 700m²/g, pore volume in the range of from about 0.1 to about 4.0 cc/g andaverage particle size in the range of from about 5 to about 500 μm. Morepreferably, the surface area of the support material is in the range offrom about 50 to about 500 m²/g, pore volume of from about 0.5 to about3.5 cc/g and average particle size of from about 10 to about 200 μm.Most preferably the surface area of the support material is in the rangeis from about 100 to about 400 m²/g, pore volume from about 0.8 to about3.0 cc/g and average particle size is from about 5 to about 100 μm. Theaverage pore size of the support material useful in the invention is inthe range of from 10 to 1000 Å, preferably 50 to about 500 Å, and mostpreferably 75 to about 350 Å. In some embodiments, the support materialis a high surface area, amorphous silica (surface area=300 m²/gm; porevolume of 1.65 cm³/gm). Preferred silicas are marketed under thetradenames of DAVISON 952 or DAVISON 955 by the Davison ChemicalDivision of W.R. Grace and Company. In other embodiments DAVISON 948 isused.

The support material should be dry, that is, free of absorbed water.Drying of the support material can be effected by heating or calciningat about 100° C. to about 1000° C., preferably at least about 600° C.When the support material is silica, it is heated to at least 200° C.,preferably about 200° C. to about 850° C., and most preferably at about600° C.; and for a time of about 1 minute to about 100 hours, from about12 hours to about 72 hours, or from about 24 hours to about 60 hours.The calcined support material must have at least some reactive hydroxyl(OH) groups to produce supported catalyst systems of this invention. Thecalcined support material is then contacted with at least onepolymerization catalyst comprising at least one metallocene compound andan activator.

The support material, having reactive surface groups, typically hydroxylgroups, is slurried in a non-polar solvent and the resulting slurry iscontacted with a solution of a metallocene compound and an activator. Insome embodiments, the slurry of the support material is first contactedwith the activator for a period of time in the range of from about 0.5hours to about 24 hours, from about 2 hours to about 16 hours, or fromabout 4 hours to about 8 hours. The solution of the metallocene compoundis then contacted with the isolated support/activator. In someembodiments, the supported catalyst system is generated in situ. Inalternate embodiment, the slurry of the support material is firstcontacted with the catalyst compound for a period of time in the rangeof from about 0.5 hours to about 24 hours, from about 2 hours to about16 hours, or from about 4 hours to about 8 hours. The slurry of thesupported metallocene compound is then contacted with the activatorsolution.

The mixture of the metallocene, activator and support is heated to about0° C. to about 70° C., preferably to about 23° C. to about 60° C.,preferably at room temperature. Contact times typically range from about0.5 hours to about 24 hours, from about 2 hours to about 16 hours, orfrom about 4 hours to about 8 hours.

Suitable non-polar solvents are materials in which all of the reactantsused herein, i.e., the activator, and the metallocene compound, are atleast partially soluble and which are liquid at reaction temperatures.Preferred non-polar solvents are alkanes, such as isopentane, hexane,n-heptane, octane, nonane, and decane, although a variety of othermaterials including cycloalkanes, such as cyclohexane, aromatics, suchas benzene, toluene, and ethylbenzene, may also be employed.

Polymerization Processes

In embodiments herein, the invention relates to polymerization processeswhere monomer (such as propylene and or ethylene), and optionallycomonomer, are contacted with a catalyst system comprising an activatorand at least one metallocene compound, as described above. The catalystcompound and activator may be combined in any order, and are combinedtypically prior to contacting with the monomer.

Monomers useful herein include substituted or unsubstituted C₂ to C₄₀alpha olefins, preferably C₂ to C₂₀ alpha olefins, preferably C₂ to C₁₂alpha olefins, preferably ethylene, propylene, butene, pentene, hexene,heptene, octene, nonene, decene, undecene, dodecene and isomers thereof.In a preferred embodiment, the monomer comprises ethylene and anoptional comonomers comprising one or more C₃ to C₄₀ olefins, preferablyC₄ to C₂₀ olefins, or preferably C₆ to C₁₂ olefins. The C₃ to C₄₀ olefinmonomers may be linear, branched, or cyclic. The C₃ to C₄₀ cyclicolefins may be strained or unstrained, monocyclic or polycyclic, and mayoptionally include heteroatoms and/or one or more functional groups.

Exemplary C₂ to C₄₀ olefin monomers and optional comonomers includeethylene, propylene, butene, pentene, hexene, heptene, octene, nonene,decene, undecene, dodecene, norbomene, norbomadiene, dicyclopentadiene,cyclopentene, cycloheptene, cyclooctene, cyclooctadiene, cyclododecene,7-oxanorbornene, 7-oxanorbornadiene, substituted derivatives thereof,and isomers thereof, preferably hexene, heptene, octene, nonene, decene,dodecene, cyclooctene, 1,5-cyclooctadiene, 1-hydroxy-4-cyclooctene,1-acetoxy-4-cyclooctene, 5-methylcyclopentene, cyclopentene,dicyclopentadiene, norbomene, norbomadiene, and their respectivehomologs and derivatives, preferably norbomene, norbomadiene, anddicyclopentadiene.

In a preferred embodiment one or more dienes are present in the polymerproduced herein at up to 10 weight %, preferably at 0.00001 to 1.0weight %, preferably 0.002 to 0.5 weight %, even more preferably 0.003to 0.2 weight %, based upon the total weight of the composition. In someembodiments 500 ppm or less of diene is added to the polymerization,preferably 400 ppm or less, preferably or 300 ppm or less. In otherembodiments at least 50 ppm of diene is added to the polymerization, or100 ppm or more, or 150 ppm or more.

Preferred diolefin monomers useful in this invention include anyhydrocarbon structure, preferably C₄ to C₃₀, having at least twounsaturated bonds, wherein at least two of the unsaturated bonds arereadily incorporated into a polymer by either a stereospecific or anon-stereospecific catalyst(s). It is further preferred that thediolefin monomers be selected from alpha, omega-diene monomers (i.e.di-vinyl monomers). More preferably, the diolefin monomers are lineardi-vinyl monomers, most preferably those containing from 4 to 30 carbonatoms. Examples of preferred dienes include butadiene, pentadiene,hexadiene, heptadiene, octadiene, nonadiene, decadiene, undecadiene,dodecadiene, tridecadiene, tetradecadiene, pentadecadiene,hexadecadiene, heptadecadiene, octadecadiene, nonadecadiene, icosadiene,heneicosadiene, docosadiene, tricosadiene, tetracosadiene,pentacosadiene, hexacosadiene, heptacosadiene, octacosadiene,nonacosadiene, triacontadiene, particularly preferred dienes include1,6-heptadiene, 1,7-octadiene, 1,8-nonadiene, 1,9-decadiene,1,10-undecadiene, 1,11-dodecadiene, 1,12-tridecadiene,1,13-tetradecadiene, and low molecular weight polybutadienes (Mw lessthan 1000 g/mol). Preferred cyclic dienes include cyclopentadiene,vinylnorbornene, norbornadiene, ethylidene norbornene, divinylbenzene,dicyclopentadiene or higher ring containing diolefins with or withoutsubstituents at various ring positions.

Preferably the comonomer(s) are present in the copolymer at less than 50mol %, preferably from 0.5 to 45 mol %, preferably from 1 to 30 mol %,preferably from 3 to 25 mol %, preferably from 5 to 20 mol %, preferablyfrom 7 to 15 mol %, with the balance of the copolymer being made up ofthe main monomer (such as propylene).

Polymerization processes of this invention can be carried out in anymanner known in the art. Any suspension, homogeneous, bulk, solution,slurry, or gas phase polymerization process known in the art can beused. Such processes can be run in a batch, semi-batch, or continuousmode. Homogeneous polymerization processes and slurry processes arepreferred. (A homogeneous polymerization process is defined to be aprocess where at least 90 wt % of the product is soluble in the reactionmedia.) A bulk homogeneous process is particularly preferred. (A bulkprocess is defined to be a process where monomer concentration in allfeeds to the reactor is 70 volume % or more.) Alternately, no solvent ordiluent is present or added in the reaction medium, (except for thesmall amounts used as the carrier for the catalyst system or otheradditives, or amounts typically found with the monomer; e.g., propane inpropylene). In another embodiment, the process is a slurry process. Asused herein the term “slurry polymerization process” means apolymerization process where a supported catalyst is employed andmonomers are polymerized on the supported catalyst particles. At least95 wt % of polymer products derived from the supported catalyst are ingranular form as solid particles (not dissolved in the diluent).

Suitable diluents/solvents for polymerization include non-coordinating,inert liquids. Examples include straight and branched-chainhydrocarbons, such as isobutane, butane, pentane, isopentane, hexanes,isohexane, heptane, octane, dodecane, and mixtures thereof; cyclic andalicyclic hydrocarbons, such as cyclohexane, cycloheptane,methylcyclohexane, methylcycloheptane, and mixtures thereof, such as canbe found commercially (Isopar™); perhalogenated hydrocarbons, such asperfluorinated C₄₋₁₀ alkanes, chlorobenzene, and aromatic andalkylsubstituted aromatic compounds, such as benzene, toluene,mesitylene, and xylene. Suitable solvents also include liquid olefinswhich may act as monomers or comonomers including ethylene, propylene,1-butene, 1-hexene, 1-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene,1-octene, 1-decene, and mixtures thereof. In a preferred embodiment,aliphatic hydrocarbon solvents are used as the solvent, such asisobutane, butane, pentane, isopentane, hexanes, isohexane, heptane,octane, dodecane, and mixtures thereof; cyclic and alicyclichydrocarbons, such as cyclohexane, cycloheptane, methylcyclohexane,methylcycloheptane, and mixtures thereof. In another embodiment, thesolvent is not aromatic, preferably aromatics are present in the solventat less than 1 wt %, preferably less than 0.5 wt %, preferably less than0 wt % based upon the weight of the solvents.

In a preferred embodiment, the feed concentration of the monomers andcomonomers for the polymerization is 60 vol% solvent or less, preferably40 vol% or less, or preferably 20 vol% or less, based on the totalvolume of the feedstream. Preferably the polymerization is run in a bulkprocess.

Preferred polymerizations can be run at any temperature and/or pressuresuitable to obtain the desired polymers. Typical temperatures and/orpressures include a temperature in the range of from about 0° C. toabout 300° C., preferably about 20° C. to about 200° C., preferablyabout 35° C. to about 150° C., preferably from about 40° C. to about120° C., preferably from about 45° C. to about 80° C.; and at a pressurein the range of from about 0.35 MPa to about 20 MPa, preferably fromabout 0.45 MPa to about 16 MPa, or preferably from about 0.5 MPa toabout 12 MPa.

In a typical polymerization, the run time of the reaction is up to 300minutes, preferably in the range of from about 5 to 250 minutes, orpreferably from about 10 to 120 minutes.

In a some embodiments hydrogen is present in the polymerization reactorat a partial pressure of 0.001 to 50 psig (0.007 to 345 kPa), preferablyfrom 0.01 to 25 psig (0.07 to 172 kPa), more preferably 0.1 to 10 psig(0.7 to 70 kPa).

In an alternate embodiment, the activity of the catalyst is at least 50g/mmol/hour, preferably 500 or more g/mmol/hour, preferably 5000 or moreg/mmol/hr, preferably 50,000 or more g/mmol/hr, preferably 100,000 ormore g/mmol/hr. In an alternate embodiment, the conversion of olefinmonomer is at least 10%, based upon polymer yield and the weight of themonomer entering the reaction zone, preferably 20% or more, preferably30% or more, preferably 50% or more, preferably 80% or more.

In an embodiment of the invention, little or no alumoxane is used in theprocess to produce the polymers. Preferably, alumoxane is present atzero mol %, alternately the alumoxane is present at a molar ratio ofaluminum to transition metal 500:1 or less, preferably 300:1 or less,preferably 100:1 or less.

In an embodiment of the invention, little or no scavenger is used in theprocess to produce the polymer. The scavenger may be present at a molarratio of scavenger metal to transition metal of less than 100:1,preferably less than 50:1, preferably less than 20:1, preferably lessthan 10:1.

In a preferred embodiment, the polymerization: 1) is conducted attemperatures of 0 to 300° C. (preferably 25 to 150° C., preferably 40 to120° C., preferably 45 to 80° C.); 2) is conducted at a pressure ofatmospheric pressure to 20 MPa (preferably 0.35 to 16 MPa, preferablyfrom 0.45 to 12 MPa, preferably from 0.5 to 10 MPa); 3) is conducted inan aliphatic hydrocarbon solvent (such as isobutane, butane, pentane,isopentane, hexanes, isohexane, heptane, octane, dodecane, and mixturesthereof; cyclic and alicyclic hydrocarbons, such as cyclohexane,cycloheptane, methylcyclohexane, methylcycloheptane, and mixturesthereof; preferably where aromatics are preferably present in thesolvent at less than 1 wt %, preferably less than 0.5 wt %, preferablyat 0 wt % based upon the weight of the solvents) or aromatic solventssuch as toluene, benzene or xylenes; 4) wherein the catalyst system usedin the polymerization comprises less than 0.5 mol %, preferably 0 mol %alumoxane, alternately the alumoxane is present at a molar ratio ofaluminum to transition metal 500:1 or less, preferably 300:1 or less,preferably 100:1 or less,) the polymerization preferably occurs in onereaction zone; 6) the productivity of the catalyst compound is at least80,000 g/mmol/hr (preferably at least 150,000 g/mmol/hr, preferably atleast 200,000 g/mmol/hr, preferably at least 250,000 g/mmol/hr,preferably at least 300,000 g/mmol/hr); 7) optionally scavengers (suchas trialkyl aluminum compounds) are absent (e.g. present at zero mol %,alternately the scavenger is present at a molar ratio of scavenger metalto transition metal of less than 100:1, preferably less than 50:1,preferably less than 20:1, preferably less than 10:1); and 8) optionallyhydrogen is present in the polymerization reactor at a partial pressureof 0.001 to 50 psig (0.007 to 345 kPa) (preferably from 0.01 to 25 psig(0.07 to 172 kPa), more preferably 0.1 to 10 psig (0.7 to 70 kPa)). In apreferred embodiment, the catalyst system used in the polymerizationcomprises no more than one catalyst compound. A “reaction zone” alsoreferred to as a “polymerization zone” is a vessel where polymerizationtakes place, for example a batch reactor. When multiple reactors areused in either series or parallel configuration, each reactor isconsidered as a separate polymerization zone. For a multi-stagepolymerization in both a batch reactor and a continuous reactor, eachpolymerization stage is considered as a separate polymerization zone. Ina preferred embodiment, the polymerization occurs in one reaction zone.Room temperature is 23° C. unless otherwise noted.

Other additives may also be used in the polymerization, as desired, suchas one or more scavengers, promoters, modifiers, chain transfer agents(such as diethyl zinc), reducing agents, oxidizing agents, hydrogen,aluminum alkyls, or silanes.

In a preferred embodiment of the invention, higher reactor temperatures,such as 70 to 150° C. and Bulky activators, such N,N-dimethylaniliniumtetrakis (perfluoronaphthyl)borate are used.

Polyolefin Products

This invention also relates to compositions of matter produced by themethods described herein.

Generally, the process of this invention produces olefin polymers,preferably polypropylene homopolymers and ethylene-propylyenecopolymers.

In an embodiment, this invention relates to a branchedpropylene-ethylene copolymer having 1) 20 wt. % ethylene or less(alternatively 15 wt. % ethylene or less, alternatively 10 wt. %ethylene or less), 2) a Tm of 50° C. or more (alternatively 70° C. ormore, alternatively 80° C. or more, alternatively 90° C. or more,alternatively 100° C. or more, alternatively 110° C. or more); and 3)greater than 75% vinyl chain ends (relative to the total unsaturatedchain ends) (alternatively greater than 80% vinyl chain ends,alternatively greater than 85% vinyl chain ends).

In a preferred embodiment, the monomer is propylene and the comonomer isethylene, preferably from 0.5 to 50 mole % ethylene, alternately 1 to 40mole %, alternately 1 to 30% mole, alternately 1 to 25 mole %,alternately 1 to 20 mole %, alternatively 1 to 15 mole %, alternately 1to 10 mole %.

In a preferred embodiment, the monomer is propylene and the comonomer isethylene, preferably from 0.5 to 50 wt. % ethylene, alternately 1 to 40wt. %, alternately 1 to 30 wt. %, alternately 1 to 25 wt. %, alternately1 to 20 wt. %, alternatively 1 to 15 wt. %, alternately 1 to 10 wt %.

In a preferred embodiment, the monomer is propylene and the comonomer isethylene, preferably from 0.5 to 50 mole % ethylene, alternately 1 to 40mole %, alternately 1 to mole 30%, alternately 1 to mole 20%,alternately 1 to 10 mole %; and the propylene-ethylene copolymercontains greater than 50% vinyl unsaturation, alternately greater than60% vinyl unsaturation, alternately greater than 70% vinyl unsaturation,alternately greater than 80% vinyl unsaturation, alternately greaterthan 90% vinyl unsaturation, alternately greater than 95% vinylunsaturation. Percent vinyl unsaturation is relative to totalunsaturated chain ends.

In a preferred embodiment, the monomer is propylene and no comonomer ispresent.

In a preferred embodiment, the monomer is propylene, no comonomer ispresent, and the polymer is isotactic.

In a preferred embodiment, the propylene homopolymer contains greaterthan 50% vinyl unsaturation, alternately greater than 60% vinylunsaturation, alternately greater than 70% vinyl unsaturation,alternately greater than 80% vinyl unsaturation, alternately greaterthan 90% vinyl unsaturation, alternately greater than 95% vinylunsaturation. Percent vinyl unsaturation is relative to totalunsaturated chain ends.

Typically, the polymers produced herein have an Mw of 3,000 to 300,000g/mol (preferably 5,000 to 200,000 g/mol, preferably 10,000 to 150,000g/mol, preferably 10,000 to 100,000 g/mol, and/or an Mw/Mn of greaterthan 1 to 40 (alternately 1.2 to 20, alternately 1.3 to 10, alternately1.4 to 5, 1.5 to 4, alternately 1.5 to 3).

In a preferred embodiment the polymer produced herein has a unimodal ormultimodal molecular weight distribution (MWD=Mw/Mn) as determined byGel Permeation Chromatography (GPC). By “unimodal” is meant that the GPCtrace has one peak or inflection point. By “multimodal” is meant thatthe GPC trace has at least two peaks or inflection points. An inflectionpoint is that point where the second derivative of the curve changes insign (e.g., from negative to positive or vice versus).

In a preferred embodiment the copolymers produced herein have acomposition distribution breadth index (CDBI) of 50% or more, preferably60% or more, preferably 70% or more. CDBI is a measure of thecomposition distribution of monomer within the polymer chains and ismeasured by the procedure described in PCT publication WO 93/03093,published Feb. 18, 1993, specifically columns 7 and 8 as well as in Wildet al, J. Poly. Sci., Poly. Phys. Ed., Vol. 20, p. 441 (1982) and U.S.Pat. No. 5,008,204, including that fractions having a weight averagemolecular weight (Mw) below 10,000 g/mol are ignored when determiningCDBI.

In a preferred embodiment of the invention, the polymer produced hereinis isotactic, preferably highly isotactic. An “isotactic” polymer has atleast 10% isotactic pentads, a “highly isotactic” polymer has at least50% isotactic pentads, and a “syndiotactic” polymer has at least 10%syndiotactic pentads, according to analysis by ¹³C-NMR. Preferablyisotactic polymers have at least 25% (preferably at least 50%,preferably at least 70%, preferably at least 80%, preferably at least90%) isotactic pentads. A polyolefin is “atactic” if it has less than 5%isotactic pentads and less than 5% syndiotactic pentads.

In an embodiment of the invention, the polymer produced herein has an mmtriad tacticity index of 75% or greater (preferably 80% or greater,preferably 85% or greater, preferably 90% or greater, preferably 95% orgreater, as determined by Carbon 13 NMR as described below.

In a preferred embodiment of the invention, the polymer produced hereinis isotactic, and contains 2,1- or 1,3-regiodefects (1,3-regiodefectsare also sometimes called 3,1-regiodefects, and the term regiodefect isalso called regioerror). In some embodiments of the invention,regiodefects are desired and advantageous, and in particular1,3-regiodefects are desired. Isotactic polymers with high levels ofregiodefects have properties similar to propylene-ethylene copolymerscontaining low levels of ethylene. In some embodiments of the invention,the polymer produced herein has 20 to 300 total regiodefects/10,000propylene units (defined as the sum of 2,1-erythro and 2,1-threoinsertions, and 3,1-isomerizations (also called 1,3-insertions) asmeasured by ¹³C-NMR) (preferably 30 to 200 total regiodefects/10,000propylene units, preferably, 50 to 150 total regiodefects/10,000propylene units).

In a preferred embodiment, the isotactic polypropylene polymer has1,3-regiodefects of at least 60/10,000 C or greater as determined by ¹³CNMR.

In a preferred embodiment, the isotactic polypropylene polymer has2,1-regiodefects of 10/10,000 C or less as determined by ¹³C NMR.

In a preferred embodiment, the isotactic polypropylene polymer has1,3-regiodefects of at least 30/10,000C or greater and stereodefects ofat least 100/10,000 C or greater as determined by ¹³C NMR.

In a preferred embodiment of the invention, the polymer produced hereinis an ethylene-propylene copolymer, and the copolymer is blocky. Ablocky copolymer is one in which the product of the reactivity ratios(r₁r₂) is greater than 1. A copolymerization between monomers “E” and“P” in the presence of catalyst “M” can be represented by the followingreaction schemes and rate equations where R₁₁ is the rate of “E”insertion after “E”, R₁₂ is the rate of “P” insertion after “E”, R₂₁ isthe rate of “E” insertion after “P”, R₂₂ is the rate of “P” insertionafter “P”, and k₁₁, k₁₂, k₂₁, and k₂₂ are the corresponding rateconstants for each. The reactions scheme and rate equations areillustrated below.

M-E+E→M-E-E R₁₁=k₁₁[ME][E]

M-E+P→M-P-E R₁₂=k₁₂[M-E][P]

M-P+E→M-E-P R₂₁=k₂₁[M-P][E]

M-P+P→M-P-P R₂₂=k₂₁[M-P][P]

The reactivity ratios r₁ and r₂ are:

$r_{1} = {{\frac{k_{11}}{k_{12}}\mspace{14mu} r_{2}} = \frac{k_{22}}{k_{21}}}$${r_{1}r_{2}} = \frac{k_{11}k_{22}}{k_{12}k_{21}}$

The product of r₁ x r₂ provides information on how the differentmonomers distribute themselves along the polymer chain. Below, areillustrations of alternating, random and blocky copolymers and how theproduct of r₁ x r₂ relates to each

-   -   r₁r₂=0 alternating copolymerization EPEPEPEPEPEPEPEPEPEP    -   r₁r₂=1 random copolymerization PPEPEPEPPEPPPEEPEEPE    -   r₁r₂>1 blocky copolymerization PPPPEEEEEEPPPEEEEEPP

¹³C-NMR Spectroscopy on Polyolefins

Polypropylene microstructure is determined by ¹³C-NMR spectroscopy,including the concentration of isotactic and syndiotactic diads ([m] and[r]), triads ([mm] and [rr]), and pentads ([mmmm] and [rrrr]). Thedesignation “m” or “r” describes the stereochemistry of pairs ofcontiguous propylene groups, “m” referring to meso and “r” to racemic.Samples are dissolved in d₂−1,1,2,2-tetrachloroethane, and spectrarecorded at 125° C. using a 100 MHz (or higher) NMR spectrometer.Polymer resonance peaks are referenced to mmmm=21.8 ppm. Calculationsinvolved in the characterization of polymers by NMR are described by F.A. Bovey in POLYMER CONFORMATION AND CONFIGURATION (Academic Press, NewYork 1969) and J. Randall in POLYMER SEQUENCE DETERMINATION, ¹³C-NMRMETHOD (Academic Press, New York, 1977).

The “propylene tacticity index”, expressed herein as [m/r], iscalculated as defined in H. N. Cheng, Macromolecules, 17, p. 1950(1984). When [m/r] is 0 to less than 1.0, the polymer is generallydescribed as syndiotactic, when [m/r] is 1.0 the polymer is atactic, andwhen [m/r] is greater than 1.0 the polymer is generally described asisotactic.

The “mm triad tacticity index” of a polymer is a measure of the relativeisotacticity of a sequence of three adjacent propylene units connectedin a head-to-tail configuration. More specifically, in the presentinvention, the mm triad tacticity index (also referred to as the “mmFraction”) of a polypropylene homopolymer or copolymer is expressed asthe ratio of the number of units of meso tacticity to all of thepropylene triads in the copolymer:

${{mm}\mspace{14mu} {Fraction}} = \frac{{PPP}({mm})}{{{PPP}({mm})} + {{PPP}({mr})} + {{PPP}({rr})}}$

where PPP(mm), PPP(mr) and PPP(rr) denote peak areas derived from themethyl groups of the second units in the possible triad configurationsfor three head-to-tail propylene units, shown below in Fischerprojection diagrams:

The calculation of the mm Fraction of a propylene polymer is describedin U.S. Pat. No. 5,504,172 (homopolymer: column 25, line 49 to column27, line 26; copolymer: column 28, line 38 to column 29, line 67). Forfurther information on how the mm triad tacticity can be determined froma ¹³C-NMR spectrum, see 1) J. A. Ewen, CATALYTIC POLYMERIZATION OFOLEFINS: PROCEEDINGS OF THE INTERNATIONAL SYMPOSIUM ON FUTURE ASPECTS OFOLEFIN POLYMERIZATION, T. Keii and K. Soga, Eds. (Elsevier, 1986), pp.271-292; and 2) U.S. Patent Application Publication No. US2004/054086(paragraphs [0043] to [0054]).

Similarly m diads and r diads can be calculated as follows where mm, mrand mr are defined above:

m=mm+½ mr

r=rr+½ mr

¹³C NMR was used to determine monomer content and sequence distributionfor the ethylene-propylene copolymers using the procedure from J.C.Randall's paper: Polymer Reviews, 1989, 29:2, 201-317. The calculationsof mole % C₃, run number, average sequence length, and diad/triaddistributions were all calculated per the method established in theabove paper. Calculations for r₁r₂ were based on the equationr₁r₂=4*[EE]*[PP]/[EP]²; where [EE], [EP], [PP] are the diad molarconcentrations; E is ethylene, P is propylene. For other copolymers ofethylene, a similar methodoly is used.

In another embodiment of the invention, the propylene polymers producedherein (preferably a homopolypropylene) have regiodefects (as determinedby ¹³C NMR), based upon the total propylene monomer. Three types defectsare defined to be the regio defects: 2,1-erythro, 2,1-threo, and3,1-isomerization. The structures and peak assignments for these aregiven in [L. Resconi, L. Cavallo, A. Fait, and F. Piemontesi, Chem. Rev.2000, 100, pp. 1253-1345]. The regio defects each give rise to multiplepeaks in the carbon NMR spectrum, and these are all integrated andaveraged (to the extent that they are resolved from other peaks in thespectrum), to improve the measurement accuracy. The chemical shiftoffsets of the resolvable resonances used in the analysis are tabulatedbelow. The precise peak positions may shift as a function of NMR solventchoice.

Regio defect Chemical shift range (ppm) 2,1-erythro 42.3, 38.6, 36.0,35.9, 31.5, 30.6, 17.6, 17.2 2,1-threo 43.4, 38.9, 35.6, 34.7, 32.5,31.2, 15.4, 15.0 3,1 insertion 37.6, 30.9, 27.7

The average integral for each defect is divided by the integral for oneof the main propylene signals (CH₃, CH, CH₂), and multiplied by 10000 todetermine the defect concentration per 10000 monomers.

The polymers produced herein typically have at least 50% allyl chainends and/or 3-alkyl chain ends (preferably at least 60%, at least 70%,at least 80%, at least 90%, at least 95%, at least 98%, or at least 99%allyl chain ends and/or 3-alkyl chain ends).

An allyl chain end is represented by CH₂CH—CH₂—, as shown in theformula:

where M represents the polymer chain. “Allylic vinyl group,” “allylchain end,” “vinyl chain end,” “vinyl termination,” “allylic vinylgroup,” and “vinyl terminated” are used interchangeably in the followingdescription. The number of allyl chain ends, vinylidene chain ends,vinylene chain ends, and other unsaturated chain ends is determinedusing ¹H NMR at 120° C. using deuterated tetrachloroethane as thesolvent on an at least 250 MHz NMR spectrometer, and in selected cases,confirmed by ¹³C NMR. Resconi has reported proton and carbon assignments(neat perdeuterated tetrachloroethane used for proton spectra, while a50:50 mixture of normal and perdeuterated tetrachloroethane was used forcarbon spectra; all spectra were recorded at 100° C. on a BRUKERspectrometer operating at 500 MHz for proton and 125 MHz for carbon) forvinyl terminated oligomers in J. American Chemical Soc., 114, 1992, pp.1025-1032 that are useful herein. Allyl chain ends are reported as amolar percentage of the total number of moles of unsaturated groups(that is, the sum of allyl chain ends, vinylidene chain ends, vinylenechain ends, and the like).

A 3-alkyl chain end (where the alkyl is a C₁ to C₃₈ alkyl), alsoreferred to as a “3-alkyl vinyl end group” or a “3-alkyl vinyltermination”, is represented by the formula:

where “****” represents the polyolefin chain and R^(b) is a C₁ to C₃₈alkyl group, or a C₁ to C₂₀ alkyl group, such as methyl, ethyl, propyl,butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, andthe like. The amount of 3-alkyl chain ends is determined using ¹³C NMRas set out below.

Mn (¹H NMR) is determined according to the following NMR method. ¹H NMRdata is collected at either room temperature or 120° C. (for purposes ofthe claims, 120° C. shall be used) in a 5 mm probe using a Varianspectrometer with a ¹H frequency of 250 MHz, 400 MHz, or 500 MHz (forthe purpose of the claims, a proton frequency of 500 MHz is used and thepolymer sample is dissolved in 1,1,2,2-tetrachloroethane-d₂ (TCE-d₂) andtransferred into a 5 mm glass NMR tube). Data are recorded using amaximum pulse width of 45° C., 5 seconds between pulses and signalaveraging 120 transients. Spectral signals are integrated and the numberof unsaturation types per 1000 carbons is calculated by multiplying thedifferent groups by 1000 and dividing the result by the total number ofcarbons. Mn is calculated by dividing the total number of unsaturatedspecies into 14,000, and has units of g/mol. The chemical shift regionsfor the olefin types are defined to be between the following spectralregions.

Unsaturation Region Number of hydrogens Type (ppm) per structure Vinyl4.98-5.13 2 Vinylidene (VYD) 4.69-4.88 2 Vinylene 5.31-5.55 2Trisubstituted 5.11-5.30 1

In a preferred embodiment of the invention, the polymer produced hereinis an a propylene homopolymer, or a copolymer of ethylene and propylene,where in the copolymers comprises from 0.1 to 50 wt % ethylene) andhaving: 1) at least 50% allyl chain ends; 2) an Mw of 3000 g/mol ormore, 3) a Tm of 90° C. or more, and 4) a g′_(vis) of 0.90 or less.

In a preferred embodiment of the invention, the polymer produced hereinis a has a branching index (g′_(vis)) of 0.90 or less, preferably 0.87or less, preferably 0.85 or less, preferably 0.80 or less, preferably0.75 or less, preferably 0.70 or less, as determined by GPC, asdescribed in the Examples section below.

In a preferred embodiment of the invention, the polymer produced herein(preferably an ethylene-propylene copolymer (preferably having 70 wt %or more propylene) or a isotactic propylene polymer) has: 1) a branchingindex (g′_(vis)) of 0.90 or less (preferably 0.87 or less, preferably0.85 or less, preferably 0.80 or less, preferably 0.75 or less,preferably 0.70 or less, as determined by GPC), 2) at least 50% allylchain ends or 3-alkyl chain ends (preferably at least 60%, at least 70%,at least 80%, at least 90%, at least 95%, at least 98%, or at least 99%allyl chain ends or 3-alkyl chain ends), 3) an Mw from 3,000 to 300,000g/mol, alternately from 5,000 to 200,000 g/mol, alternately 10,000 to150,000 g/mol, alternately 20,000 to 100,000 g/mol; and 4) a Tm of 90°C. or more, alternately 100° C. or more, alternately 110° C. or more,alternately 115° C. or more, alternately 120° C. or more, alternately125° C. or more, preferably the polymer has at least X % vinyl chainends (relative to total unsaturations as measured by ¹H NMR, whereX=47.8*g′_(vis)+45.1 (alternately X=47.8*g′_(vis)+46.1, alternatelyX=47.8*g′_(vis)+47.1).

The polymers prepared herein may be functionalized by reacting aheteroatom containing group with the polymer with or without a catalyst.Examples include catalytic hydrosilylation, ozonolysis,hydroformylation, or hydroamination, sulfonation, halogenation,hydrohalogenation, hydroboration, epoxidation, or Diels-Alder reactionswith polar dienes, Friedel-Crafts reactions with polar aromatics,maleation with activators such as free radical generators (e.g.peroxides). The functionalized polymers can be used in oil additives, asanti-fogging or wetting additives, adhesion promoters and many otherapplications. Preferred uses include additives for lubricants and orfuels. Preferred heteroatom containing groups include, amines,aldehydes, alcohols, acids, anhydrides, sulphonates, particularlysuccinic acid, maleic acid and maleic anhydride.

Other uses of the functionalized polymers include as plasticizers,surfactants for soaps, detergents, fabric softeners, antistatics, etc.Preferred heteroatom containing groups include, amines, aldehydes,alcohols, acids, anhydrides, and sulphonates, particularly succinicacid, maleic acid and maleic anhydride.

In some embodiments the polymers produced herein are functionalized asdescribed in U.S. Pat. No. 6,022,929; A. Toyota, T. Tsutsui, and N.Kashiwa, Polymer Bulletin 48, 213-219, 2002; and J. Am. Chem. Soc.,1990, 112, 7433-7434.

Blends

In another embodiment, the polymer (preferably the polypropylene)produced herein is combined with one or more additional polymers priorto being formed into a film, molded part or other article. Other usefulpolymers include polyethylene, isotactic polypropylene, highly isotacticpolypropylene, syndiotactic polypropylene, random copolymer of propyleneand ethylene, and/or butene, and/or hexene, polybutene, ethylene vinylacetate, LDPE, LLDPE, HDPE, ethylene vinyl acetate, ethylene methylacrylate, copolymers of acrylic acid, polymethylmethacrylate or anyother polymers polymerizable by a high-pressure free radical process,polyvinylchloride, polybutene-1, isotactic polybutene, ABS resins,ethylene-propylene rubber (EPR), vulcanized EPR, EPDM, block copolymer,styrenic block copolymers, polyamides, polycarbonates, PET resins, crosslinked polyethylene, copolymers of ethylene and vinyl alcohol (EVOH),polymers of aromatic monomers such as polystyrene, poly-1 esters,polyacetal, polyvinylidine fluoride, polyethylene glycols, and/orpolyisobutylene.

In a preferred embodiment, the polymer (preferably the polypropylene) ispresent in the above blends, at from 10 to 99 wt %, based upon theweight of the polymers in the blend, preferably 20 to 95 wt %, even morepreferably at least 30 to 90 wt %, even more preferably at least 40 to90 wt %, even more preferably at least 50 to 90 wt %, even morepreferably at least 60 to 90 wt %, even more preferably at least 70 to90 wt %.

The blends described above may be produced by mixing the polymers of theinvention with one or more polymers (as described above), by connectingreactors together in series to make reactor blends or by using more thanone catalyst in the same reactor to produce multiple species of polymer.The polymers can be mixed together prior to being put into the extruderor may be mixed in an extruder.

The blends may be formed using conventional equipment and methods, suchas by dry blending the individual components and subsequently meltmixing in a mixer, or by mixing the components together directly in amixer, such as, for example, a Banbury mixer, a Haake mixer, a Brabenderinternal mixer, or a single or twin-screw extruder, which may include acompounding extruder and a side-arm extruder used directly downstream ofa polymerization process, which may include blending powders or pelletsof the resins at the hopper of the film extruder. Additionally,additives may be included in the blend, in one or more components of theblend, and/or in a product formed from the blend, such as a film, asdesired. Such additives are well known in the art, and can include, forexample: fillers; antioxidants (e.g., hindered phenolics such asIRGANOX™ 1010 or IRGANOX™ 1076 available from Ciba-Geigy); phosphites(e.g., IRGAFOS™ 168 available from Ciba-Geigy); anti-cling additives;tackifiers, such as polybutenes, terpene resins, aliphatic and aromatichydrocarbon resins, alkali metal and glycerol stearates, andhydrogenated rosins; UV stabilizers; heat stabilizers; anti-blockingagents; release agents; anti-static agents; pigments; colorants; dyes;waxes; silica; fillers; talc; and the like.

Films

Any of the foregoing polymers, including blends thereof, may be used ina variety of end-use applications. Such applications include, forexample, mono- or multi-layer blown, extruded, and/or shrink films.These films may be formed by any number of well known extrusion orcoextrusion techniques, such as a blown bubble film processingtechnique, wherein the composition can be extruded in a molten statethrough an annular die and then expanded to form a uni-axial or biaxialorientation melt prior to being cooled to form a tubular, blown film,which can then be axially slit and unfolded to form a flat film. Filmsmay be subsequently unoriented, uniaxially oriented, or biaxiallyoriented to the same or different extents. One or more of the layers ofthe film may be oriented in the transverse and/or longitudinaldirections to the same or different extents. The uniaxially orientationcan be accomplished using typical cold drawing or hot drawing methods.Biaxial orientation can be accomplished using tenter frame equipment ora double bubble process and may occur before or after the individuallayers are brought together. For example, a polyethylene layer can beextrusion coated or laminated onto an oriented polypropylene layer orthe polyethylene and to polypropylene can be coextruded together into afilm then oriented. Likewise, oriented polypropylene could be laminatedto oriented polyethylene or oriented polyethylene could be coated ontopolypropylene then optionally the combination could be oriented evenfurther. Typically the films are oriented in the Machine Direction (MD)at a ratio of up to 15, preferably between 5 and 7, and in theTransverse Direction (TD) at a ratio of up to 15, preferably 7 to 9.However, in another embodiment the film is oriented to the same extentin both the MD and TD directions.

The films may vary in thickness depending on the intended application;however, films of a thickness from 1 to 50 μm are usually suitable.Films intended for packaging are usually from 10 to 50 μm thick. Thethickness of the sealing layer is typically 0.2 to 50 μm. There may be asealing layer on both the inner and outer surfaces of the film or thesealing layer may be present on only the inner or the outer surface.

In another embodiment, one or more layers may be modified by coronatreatment, electron beam irradiation, gamma irradiation, flametreatment, or microwave. In a preferred embodiment, one or both of thesurface layers is modified by corona treatment.

Molded Products

The polymers described herein (preferably propylene polymers) and blendsthereof may also be used to prepare molded products in any moldingprocess, including but not limited to, injection molding, gas-assistedinjection molding, extrusion blow molding, injection blow molding,injection stretch blow molding, compression molding, rotational molding,foam molding, thermoforming, sheet extrusion, and profile extrusion. Themolding processes are well known to those of ordinary skill in the art.

Further, the polymers described herein (preferably propylene polymers)may be shaped into desirable end use articles by any suitable meansknown in the art. Thermoforming, vacuum forming, blow molding,rotational molding, slush molding, transfer molding, wet lay-up orcontact molding, cast molding, cold forming matched-die molding,injection molding, spray techniques, profile co-extrusion, orcombinations thereof are typically used methods.

Thermoforming is a process of forming at least one pliable plastic sheetinto a desired shape. Typically, an extrudate film of the composition ofthis invention (and any other layers or materials) is placed on ashuttle rack to hold it during heating. The shuttle rack indexes intothe oven which pre-heats the film before forming. Once the film isheated, the shuttle rack indexes back to the forming tool. The film isthen vacuumed onto the forming tool to hold it in place and the formingtool is closed. The tool stays closed to cool the film and the tool isthen opened. The shaped laminate is then removed from the tool. Thethermoforming is accomplished by vacuum, positive air pressure,plug-assisted vacuum forming, or combinations and variations of these,once the sheet of material reaches thermoforming temperatures, typicallyof from 140° C. to 185° C. or higher. A pre-stretched bubble step isused, especially on large parts, to improve material distribution.

Blow molding is another suitable forming means for use with thecompositions of this invention, which includes injection blow molding,multi-layer blow molding, extrusion blow molding, and stretch blowmolding, and is especially suitable for substantially closed or hollowobjects, such as, for example, gas tanks and other fluid containers.Blow molding is described in more detail in, for example, CONCISEENCYCLOPEDIA OF POLYMER SCIENCE AND ENGINEERING, pp. 90-92 (JacquelineI. Kroschwitz, ed., John Wiley & Sons 1990).

Likewise, molded articles may be fabricated by injecting molten polymerinto a mold that shapes and solidifies the molten polymer into desirablegeometry and thickness of molded articles. Sheets may be made either byextruding a substantially flat profile from a die, onto a chill roll, oralternatively by calendaring. Sheets are generally considered to have athickness of from 10 mils to 100 mils (254 μm to 2540 μm), although anygiven sheet may be substantially thicker.

Non-Wovens and Fibers

The polymers produced herein may also be used to prepare nonwovenfabrics and fibers in any nonwoven fabric and fiber making process,including but not limited to, melt blowing, spunbonding, filmaperturing, and staple fiber carding. A continuous filament process mayalso be used. Preferably a spunbonding process is used. The spunbondingprocess is well known in the art. Generally it involves the extrusion offibers through a spinneret. These fibers are then drawn using highvelocity air and laid on an endless belt. A calender roll is generallythen used to heat the web and bond the fibers to one another althoughother techniques may be used such as sonic bonding and adhesivebonding. 1. This invention also relates to a process for polymerization,comprising: (i) contacting one or more monomers comprising propylene andoptionally ethylene, with a catalyst system comprising a metallocenecatalyst compound and an activator, wherein the metallocene catalystcompound is represented by the formula:

where each R³ is hydrogen; each R⁴ is independently a C₁-C₁₀ alkyl; eachR² and R⁷ is independently hydrogen, or C₁-C₁₀ alkyl, each R⁵ and R⁶ isindependently hydrogen, C₁-C₅₀ substituted or unsubstituted hydrocarbyl,or C₁-0₅₀ substituted or unsubstituted halocarbyl; and R⁴ and R⁵, R⁵ andR⁶ and/or R⁶ and R⁷ may optionally be bonded together to form a ringstructure; J is a bridging group represented by the formula Ra₂J′, whereJ′ is C or Si, and each R^(a) is, independently, C₁ to C₂₀ substitutedor unsubstituted hydrocarbyl, and the two R^(a) form a cyclic structureincorporating J′ and the cyclic structure may be a saturated orpartially saturated cyclic or fused ring system; and each X is aunivalent anionic ligand, or two Xs are joined and bound to the metalatom to form a metallocycle ring, or two Xs are joined to form achelating ligand, a diene ligand, or an alkylidene ligand; and

-   -   (ii) obtaining a polymer having: 1) greater than 40% vinyl chain        ends, relative to the total unsaturated chain ends, 2) a Tm of        70° C. or more; 3) an Mw of 3000 to 300,000 g/mol, and 4) a        g′_(vis) of 0.90 or less.

2. The process of paragraph 1, wherein step (i) occurs at a temperatureof greater than 60° C. (alternatively 70° C., alternatively 80° C.,alternatively 90° C., alternatively 100° C.)

3. The process of paragraph 1, wherein the polymer produced has 1)greater than 70% vinyl chain ends, relative to total unsaturated chainends (alternatively 75%, alternatively 80%, alternatively 85%,alternatively 90%), and 2) a Mw of 3000 to 200,000 g/mole (alternatively5,000 to 150,000, alternatively 10,000 to 100,000)

4. The process of paragraph 1, 2 or 3, wherein the polymer produced isisotactic polypropylene having a Tm of 115° C. or more (alternatively120° C. or more, alternatively 125 ° C. or more).

5. The process of paragraph 1, wherein the polymer produced is apropylene-ethylene copolymer containing 30 wt % or less of ethylene(alternatively 25 wt % or less of ethylene, alternatively 20 wt % orless of ethylene, alternatively 15 wt % or less of ethylene,alternatively 10 wt % or less of ethylene).

6. The process of paragraph 1, 2, 3 or 4 wherein the polyolefin producedhas a g′_(vis) of 0.85 or less. 7. The process of paragraph 4, whereinthe polyolefin produced has at least X % vinyl chain ends (relative tototal unsaturations as measured by ¹H NMR, where X=47.8*g′_(vis)+45.1.

8. A branched polymer produced by any of the above paragraphs 1 to 7.

9. A branched isotactic polypropylene polymer having at least X % vinylchain ends (relative to total unsaturations as measured by ¹H-NMR),where X=47.8*g′_(vis)+45.1.

10. The polymer of paragraph 8 or 9 having greater than 80% vinylunsaturation (relative to total unsaturation as measured by ¹H NMR)(alternatively greater the 85%).

11. The polymer of paragraph 8, 9 or 10 having a Mw of 3000 to 100,000g/mol (alternatively 4000 to 50,000 g/mol).

12. The polymer of paragraph 8, 9, 10 or 11 having a Tm of 100° C. more(alternatively 110° C. more, alternatively 115° C. more, alternatively100° C. more, alternatively 130° C. more).

13. A branched propylene-ethylene copolymer having 1) 20 wt. % ethyleneor less (alternatively 15 wt. % ethylene or less, alternatively 10 wt. %ethylene or less), 2) a Tm of 50° C. or more (alternatively 70° C. ormore, alternatively 80° C. or more, alternatively 90° C. or more,alternatively 100° C. or more, alternatively 110° C. or more); and 3)greater than 75% vinyl chain ends (relative to the total unsaturatedchain ends) (alternatively greater than 80% vinyl chain ends,alternatively greater than 85% vinyl chain ends).

14. The polymer of paragraph 13 having a Mw of 20,000 to 300,000 g/mol(alternatively 25,000 to 250,000).

15. The process of any of paragraphs 1 to 8 wherein R², R⁴ and R⁷ are,independently, selected from the group consisting of methyl, ethyl,propyl, butyl, pentyl, heptyl, hexyl, octyl, nonyl, decyl and an isomersthereof

16. The process of any of paragraphs 1 to 8, and 15 wherein R² and R⁴are, independently, a C₁ to C₁₀ alkyl.

17. The process of any of paragraphs 1 to 8, 15 and 16 wherein R⁴ and R⁷are, independently, a C₁ to C₁₀ alkyl.

18. The process of any of paragraphs 1 to 8, 15, 16 and 17 wherein eachX is, independently, selected from the group consisting of hydrocarbylradicals having from 1 to 20 carbon atoms, hydrides, amides, alkoxides,sulfides, phosphides, halides, dienes, amines, phosphines, ethers, and acombination thereof, (two X′s may form a part of a fused ring or a ringsystem).

19. The process of any of paragraphs 1 to 8, and 15-18 wherein J isrepresented by the formula:

wherein J′ is a carbon or silicon atom, x is 1, 2, 3, or 4, and each R′is, independently, hydrogen or C₁-C₁₀ hydrocarbyl.

20. The process of any of paragraphs 1 to 8, and 15 to 19 wherein J iscyclopentamethylenesilylene, cyclotetramethylenesilylene,cyclotrimethylenesilylene.

21. The process The process of any of paragraphs 1 to 8, and 15 to 20wherein the activator comprises alumoxane, preferably present at a molarratio of aluminum to catalyst compound transition metal of 100:1 ormore.

22. The process of any of paragraphs 1 to 8, and 15 to 21 wherein theactivator comprises a non-coordinating anion activator.

23. The process of any of paragraphs 1 to 8, and 15 to 22 whereinactivator is represented by the formula:

(Z)_(d) ⁺(A^(d−))

wherein Z is (L-H) or a reducible Lewis Acid, L is an neutral Lewisbase; H is hydrogen; (L-H)⁺ is a Bronsted acid; A^(d−) is anon-coordinating anion having the charge d−; and d is an integer from 1to 3.

24. The process of any of paragraphs 1 to 8, and 15 to 22 whereinactivator is represented by the formula:

(Z)_(d) ⁺(A^(d−))

wherein A^(d−) is a non-coordinating anion having the charge d−; d is aninteger from 1 to 3, and

Z is a reducible Lewis acid represented by the formula: (Ar₃C⁺), whereAr is aryl or aryl substituted with a heteroatom, a C₁ to C₄₀hydrocarbyl, or a substituted C₁ to C₄₀ hydrocarbyl.

Experimental Gel Permeation Chromatography

Mw, Mn, Mz, number of carbon atoms and g′_(vis) are determined by usinga High Temperature Size Exclusion Chromatograph (either from WatersCorporation or Polymer Laboratories), equipped with three in-linedetectors, a differential refractive index detector (DRI), a lightscattering (LS) detector, and a viscometer. Experimental details,including detector calibration, are described in: T. Sun, P. Brant, R.R. Chance, and W. W. Graessley, Macromolecules, Volume 34, Number 19,6812-6820, (2001) and references therein. Three Polymer LaboratoriesPLgel 10 mm Mixed-B LS columns are used. The nominal flow rate is 0.5cm³/min, and the nominal injection volume is 300 μL. The varioustransfer lines, columns and differential refractometer (the DRIdetector) are contained in an oven maintained at 145° C. Solvent for theexperiment is prepared by dissolving 6 grams of butylated hydroxytoluene as an antioxidant in 4 liters of Aldrich reagent grade1,2,4trichlorobenzene (TCB). The TCB mixture is then filtered through a0.7 μm glass pre-filter and subsequently through a 0.1 μm Teflon filter.The TCB is then degassed with an online degasser before entering theSize Exclusion Chromatograph. Polymer solutions are prepared by placingdry polymer in a glass container, adding the desired amount of TCB, thenheating the mixture at 160° C. with continuous agitation for about 2hours. All quantities are measured gravimetrically. The TCB densitiesused to express the polymer concentration in mass/volume units are 1.463g/ml at room temperature and 1.324 g/ml at 145° C. The injectionconcentration is from 0.75 to 2.0 mg/ml, with lower concentrations beingused for higher molecular weight samples. Prior to running each samplethe DRI detector and the injector are purged. Flow rate in the apparatusis then increased to 0.5 ml/minute, and the DRI is allowed to stabilizefor 8 to 9 hours before injecting the first sample. The LS laser isturned on 1 to 1.5 hours before running the samples. The concentration,c, at each point in the chromatogram is calculated from thebaseline-substracted DRI signal, I_(DRI), using the following equation:

c=K _(DRI) /I _(DRI)/(dn/dc)

where K_(DRI) is a constant determined by calibrating the DRI, and(dn/dc) is the refractive index increment for the system. The refractiveindex, n=1.500 for TCB at 145° C. and □=690 nm. For purposes of thisinvention and the claims thereto (dn/dc)=0.104 for propylene polymers,0.098 for butene polymers and 0.1 otherwise. Units on parametersthroughout this description of the SEC method are such thatconcentration is expressed in g/cm³, molecular weight is expressed ing/mole, and intrinsic viscosity is expressed in dL/g.

The LS detector is a Wyatt Technology High Temperature mini-DAWN. Themolecular weight, M, at each point in the chromatogram is determined byanalyzing the LS output using the Zimm model for static light scattering(M. B. Huglin, LIGHT SCATTERING FROM POLYMER SOLUTIONS, Academic Press,1971):

$\frac{K_{O}c}{\Delta \; {R(\theta)}} = {\frac{1}{{MP}(\theta)} + {2A_{2}c}}$

Here, ΔR(θ) is the measured excess Rayleigh scattering intensity atscattering angle θ, c is the polymer concentration determined from theDRI analysis, A₂ is the second virial coefficient [for purposes of thisinvention, A₂=0.0006 for propylene polymers, 0.0015 for butene polymersand 0.001 otherwise], (dn/dc)=0.104 for propylene polymers, 0.098 forbutene polymers and 0.1 otherwise, P(θ) is the form factor for amonodisperse random coil, and K_(o) is the optical constant for thesystem:

$K_{O} = \frac{4\pi^{2}{n^{2}\left( {{dn}\text{/}{dc}} \right)}^{2}}{\lambda^{4}N_{A}}$

where N_(A) is Avogadro's number, and (dn/dc) is the refractive indexincrement for the system. The refractive index, n=1.500 for TCB at 145°C. and λ=690 nm.

A high temperature Viscotek Corporation viscometer, which has fourcapillaries arranged in a Wheatstone bridge configuration with twopressure transducers, is used to determine specific viscosity. Onetransducer measures the total pressure drop across the detector, and theother, positioned between the two sides of the bridge, measures adifferential pressure. The specific viscosity, η_(s), for the solutionflowing through the viscometer is calculated from their outputs. Theintrinsic viscosity, [η], at each point in the chromatogram iscalculated from the following equation:

η_(s) =c[η]+0.3(c[η])²

where c is concentration and was determined from the DRI output.

The branching index (g′_(vis)) is calculated using the output of theSEC-DRI-LS-VIS method as follows. The average intrinsic viscosity,[η]_(avg), of the sample is calculated by:

$\lbrack\eta\rbrack_{avg} = \frac{\Sigma \; {c_{i}\lbrack\eta\rbrack}_{i}}{\Sigma \; c_{i}}$

where the summations are over the chromatographic slices, i, between theintegration limits. The branching index g′_(vis) is defined as:

${g^{\prime}{vis}} = \frac{\lbrack\eta\rbrack_{avg}}{{kM}_{V}^{\alpha}}$

where, for purpose of this invention and claims thereto, α=0.695 andk=0.000579 for linear ethylene polymers, α=0.705 k=0.000262 for linearpropylene polymers, and α=0.695 and k=0.000181 for linear butenepolymers. M_(v) is the viscosity-average molecular weight based onmolecular weights determined by LS analysis.

Viscosity was measured using a Brookfield Viscometer according to ASTMD-3236.

Peak melting point, Tm, (also referred to as melting point), peakcrystallization temperature, Tc, (also referred to as crystallizationtemperature), glass transition temperature (Tg), heat of fusion(ΔH_(f)), and percent crystallinity were determined using the followingDSC procedure according to ASTM D3418-03. Differential scanningcalorimetric (DSC) data were obtained using a TA Instruments model Q200machine or similar machine. Samples weighing approximately 5-10 mg weresealed in an aluminum hermetic sample pan. The DSC data were recorded byfirst gradually heating the sample to 200° C. at a rate of 10°C./minute. The sample was kept at 200° C. for 2 minutes, then cooled to−90° C. at a rate of 10° C./minute, followed by an isothermal for 2minutes and heating to 200° C. at 10° C./minute. Both the first andsecond cycle thermal events were recorded. Areas under the endothermicpeaks were measured and used to determine the heat of fusion and thepercent of crystallinity. The percent crystallinity is calculated usingthe formula, [area under the melting peak (Joules/gram)/B (Joules/gram)]*100, where B is the heat of fusion for the 100% crystalline homopolymerof the major monomer component. These values for B are to be obtainedfrom the Polymer Handbook, Fourth Edition, published by John Wiley andSons, New York 1999, provided however that a value of 189 J/g (B) isused as the heat of fusion for 100% crystalline polypropylene, a valueof 290 J/g is used for the heat of fusion for 100% crystallinepolyethylene. The melting and crystallization temperatures reported herewere obtained during the second heating/cooling cycle unless otherwisenoted. This DSC technique described was used for polymers produced fromcontinuous stirred tank reactor runs.

MFR (dg/min) is determined according to ASTM 1238 using a load of 2.16kg and at a temperature of 230 C.

List of Catalysts

Compounds used in the following polymerization examples include:

The above compounds were prepared according to the general proceduresdescribed in U.S. Ser. No. 61/847,441, filed Jul. 17, 2013.

Comparative compounds used in the following polymerization examplesinclude:

-   rac-(PhC₂H₄)₂Si(4,7-Me₂Ind)₂HfMe₂ (Catalyst ID in table 1, C-A)-   rac-(n-C₆H₁₃)₂Si[4,7-Me₂Ind]₂HfMe₂ (Catalyst ID in table 1, C-B)-   rac-(Me₂Si)₂[4,7-Me₂Ind]₂HfMe₂ (Catalyst ID in table 1, C-C)-   rac-CH₂CH₂[5-t-Bu-7-MeInd]₂HfMe₂ (Catalyst ID in table 1, C-D)-   rac-Me₂Si[2-Me-4-PhInd]₂ZrMe₂ (Catalyst ID in tables 1, C-E)-   rac-Me₂Si[2-Me-3-nPrInd]2HfMe₂ (Catalyst ID in table 1, C-F)-   rac-Me₂Si[Ind]₂HfMe₂ (Catalyst ID in table 1, C-G),-   wherein Ind=indenyl, Me=methyl, n-C₆H₁₃=n-hexyl, nPr=n-propyl,    Ph=phenyl, PhC₂H₄=phenethyl, tBu=tert-butyl, CH₂CH₂=ethylene.

High Throughput Polymerization Examples

Solutions of the pre-catalysts were made using toluene (ExxonMobilChemical Company anhydrous, stored under N₂) (98%). Pre-catalystsolutions were typically 0.5 mmol/L. When noted, some pre-catalysts werepre-alkylated using triisobutyl aluminum (TiBAl, neat, AkzoNobel);prealkylation was performed by first dissolving the pre-catalyst in theappropriate amount of toluene, and then adding 20 equivalents of TiBAlsuch that the final pre-catalyst solution was 0.5 mmol precatalyst/L and10 mmol TiBAl/L.

Solvents, polymerization grade toluene and/or isohexanes were suppliedby ExxonMobil Chemical Co. and are purified by passing through a seriesof columns: two 500 cc Oxyclear cylinders in series from Labclear(Oakland, Calif), followed by two 500 cc columns in series packed withdried 3 Å mole sieves (8-12 mesh; Aldrich Chemical Company), and two 500cc columns in series packed with dried 5 Å mole sieves (8-12 mesh;Aldrich Chemical Company).

Polymerization grade ethylene was used and further purified by passingit through a series of columns: 500 cc Oxyclear cylinder from Labclear(Oakland, Calif) followed by a 500 cc column packed with dried 3 Å molesieves (8-12 mesh; Aldrich Chemical Company), and a 500 cc column packedwith dried 5 mole sieves (8-12 mesh; Aldrich Chemical Company).

Polymerization grade propylene was used and further purified by passingit through a series of columns: 2250 cc Oxiclear cylinder from Labclearfollowed by a 2250 cc column packed with 3 Å mole sieves (8-12 mesh;Aldrich Chemical Company), then two 500 cc columns in series packed with5 Å mole sieves (8-12 mesh; Aldrich Chemical Company), then a 500 cccolumn packed with Selexsorb CD (BASF), and finally a 500 cc columnpacked with Selexsorb COS (BASF).

Activation of the pre-catalysts was either by methylalumoxane (MAO, 10wt % in toluene, Albemarle Corp.), dimethylaniliniumtetrakisperfluorophenylborate (Boulder Scientific and Albemarle Corp) ordimethylanilinium tetrakis(perfluoronaphthyl)borate (Albemarle Corp).MAO was used as a 0.5 wt % or 1.0 wt % in toluene solution. Micromolesof MAO reported in the experimental section are based on the micromolesof aluminum in MAO. The formula weight of MAO is 58.0 grams/mole.Dimethylanilinium tetrakisperfluorophenylborate and dimethylaniliniumtetrakis(perfluoronaphthyl)borate were typically used as a 5 mmol/Lsolution in toluene.

For polymerization runs using dimethylaniliniumtetrakisperfluorophenylborate or dimethylaniliniumtetrakis(perfluoronaphthyl)borate, tri-n-octylaluminum (TnOAl, Neat,AkzoNobel) was also used as a scavenger prior to introduction of theactivator and pre-catalyst into the reactor. TnOAl was typically used asa 5 mmol/L solution in toluene.

Reactor Description and Preparation:

Polymerizations were conducted in an inert atmosphere (N₂) drybox usingautoclaves equipped with an external heater for temperature control,glass inserts (internal 22.5 mL for C₃ and C₂/C₃ runs), septum inlets,regulated supply of nitrogen, ethylene and propylene, and equipped withdisposable PEEK mechanical stirrers (800 RPM). The autoclaves wereprepared by purging with dry nitrogen at 110° C. or 115° C. for 5 hoursand then at 25° C. for 5 hours.

Propylene Polymerization (PP):

The reactor was prepared as described above, then heated to 40° C., andthen purged with propylene gas at atmospheric pressure. For MAOactivated runs, toluene or isohexane, MAO, and liquid propylene (1.0 mL)were added via syringe. The reactor was then heated to processtemperature (70° C. or 100° C.) while stirring at 800 RPM. Thepre-catalyst solution was added via syringe with the reactor at processconditions. For dimethylanilinium tetrakisperfluorophenylborate ordimethylanilinium tetrakisperfluoronaphthylborate activated runs,isohexanes, liquid propylene (1.0 mL) and scavenger (TnOAl, 0.5 μmol)were added via syringe. The reactor was then brought to processtemperature (70° C. or 100° C.) while stirring at 800 RPM. The activatorsolution, followed by the pre-catalyst solution, were injected viasyringe to the reactor at process conditions. Reactor temperature wasmonitored and typically maintained within +/−1° C. Polymerizations werehalted by addition of approximately 50 psi O₂/Ar (5 mole % O₂) gasmixture to the autoclaves for approximately 30 seconds. Thepolymerizations were quenched based on a predetermined pressure loss ofapproximately 8-20 psi (max quench value in psi) or for a maximum of 30minutes polymerization time for experiments listed in Table 2, or for amaximum of 45 minutes polymerization time for experiments listed inTable 1. The reactors were cooled and vented. The polymers were isolatedafter the solvent was removed in-vacuo. The actual quench time (s) andmax quench value (psi) are reported. Yields reported include totalweight of polymer and residual catalyst. Catalyst activity is reportedas grams of polymer per mmol transition metal compound per hour ofreaction time (g/mmol·hr). Propylene homopolymerization examples arereported in Table 1 (Ex# starting with PP or CPP only) and in Table 2.

Ethylene-Propylene Copolymerization (EP):

The reactor was prepared as described above, then heated to 40° C. andthen purged with ethylene gas at atmospheric pressure. The listedethylene pressure (10, 20, 40, 60 or 80 psid) was then added to thereactor. Isohexanes and scavenger (TnOAl, 0.5 μmol) were added viasyringe. The stirrers were then started and maintained at 800 RPM.Liquid propylene (1.0 ml) was then injected into the reactor. Thereactor was then brought to process temperature (70° C.). The activatorsolution, followed by the pre-catalyst solution, was injected viasyringe to the reactor at process conditions. Reactor temperature wasmonitored and typically maintained within +/−1° C. Polymerizations werehalted by addition of approximately 50 psi O₂/Ar (5 mole % O₂) gasmixture to the autoclaves for approximately 30 seconds. Thepolymerizations were quenched based on a predetermined pressure loss ofapproximately 10-20 psi or for a maximum of 45 minutes polymerizationtime. The reactors were cooled and vented. The polymer was isolatedafter the solvent was removed in-vacuo. The quench time (s) and maxquench value (psi) are reported in Table 1 for each run. Yields reportedinclude total weight of polymer and residual catalyst. Catalyst activityis reported as grams of polymer per mmol transition metal compound perhour of reaction time (g/mmol·hr). Ethylene/propylene copolymerizationexamples are collected in Table 1.

High Throughput Polymer Characterization

For analytical testing, polymer sample solutions were prepared bydissolving polymer in 1,2,4-trichlorobenzene (TCB, 99+% purity fromSigma-Aldrich) containing 2,6-di-tert-butyl-4-methylphenol (BHT, 99%from Aldrich) at 165° C. in a shaker oven for approximately 3 hours. Thetypical concentration of polymer in solution was between 0.1 to 0.9mg/mL with a BHT concentration of 1.25 mg BHT/mL of TCB. Samples werecooled to 135° C. for testing.

High temperature size exclusion chromatography was performed using anautomated “Rapid GPC” system as described in U.S. Pat. Nos. 6,491,816;6,491,823; 6,475,391; 6,461,515; 6,436,292; 6,406,632; 6,175,409;6,454,947; 6,260,407; and 6,294,388; each of which is incorporatedherein by reference. Molecular weights (weight average molecular weight(Mw) and number average molecular weight (Mn)) and molecular weightdistribution (MWD=Mw/Mn), which is also sometimes referred to as thepolydispersity (PDI) of the polymer, were measured by Gel PermeationChromatography using a Symyx Technology GPC equipped with evaporativelight scattering detector and calibrated using polystyrene standards(Polymer Laboratories: Polystyrene Calibration Kit S-M-10: Mp (peak Mw)between 5000 and 3,390,000). Samples (250 μL of a polymer solution inTCB were injected into the system) were run at an eluent flow rate of2.0 mL/minute (135° C. sample temperatures, 165° C. oven/columns) usingthree Polymer Laboratories: PLgel 10 μm Mixed-B 300×7.5mm columns inseries. No column spreading corrections were employed. Numericalanalyses were performed using Epoch® software available from SymyxTechnologies. The molecular weights obtained are relative to linearpolystyrene standards. Molecular weight data is reported in Tables 1 and2 under the headings Mn, Mw and PDI as defined above.

Differential Scanning calorimetry (DSC) measurements were performed on aTA-Q100 instrument to determine the melting point of the polymers.Samples were pre-annealed at 220° C. for 15 minutes and then allowed tocool to room temperature overnight. The samples were then heated to 220°C. at a rate of 100° C./minute and then cooled at a rate of 50°C./minute. Melting points were collected during the heating period. Theresults are reported in the Tables 1 and 2 under the heading, T_(m) (°C.).

Samples for infrared analysis were prepared by depositing the stabilizedpolymer solution onto a silanized wafer (Part number S10860, Symyx). Bythis method, approximately between 0.12 and 0.24 mg of polymer isdeposited on the wafer cell. The samples were subsequently analyzed on aBrucker Equinox 55 FTIR spectrometer equipped with Pikes' MappIRspecular reflectance sample accessory. Spectra, covering a spectralrange of 5000 cm⁻¹ to 500 cm⁻¹, were collected at a 2 cm⁻¹ resolutionwith 32 scans.

For ethylene-propylene copolymers, the wt. % ethylene is determined viameasurement of the methylene rocking band (˜770 cm⁻¹ to 700 cm−1). Thepeak area of this band is normalized by sum of the band areas of thecombination and overtone bands in the 4500 cm⁻¹ to 4000 cm⁻¹ range. Thenormalized band area is then correlated to a calibration curve from ¹³CNMR data to predict the wt. % ethylene within a concentration range of˜5 to 40 wt. %. Typically, R² correlations of 0.98 or greater areachieved. These numbers are reported in Table 1 under the heading C2 wt.%.

¹³C NMR spectroscopy was used to characterize some polypropylene polymersamples produced in experiments collected in Table 3. Unless otherwiseindicated the polymer samples for ¹³C NMR spectroscopy were dissolved ind₂-1,1,2,2-tetrachloroethane and the samples were recorded at 125° C.using a NMR spectrometer with a ¹³C NMR frequency of 150 MHz. Polymerresonance peaks are referenced to mmmm=21.8 ppm. Calculations involvedin the characterization of polymers by NMR follow the work of F. A.Bovey in “Polymer Conformation and Configuration” Academic Press, NewYork 1969 and J. Randall in “Polymer Sequence Determination, Carbon-13NMR Method”, Academic Press, New York, 1977.

The stereodefects measured as “stereo defects/10,000 monomer units” arecalculated from the sum of the intensities of mmrr, mmrm+rrmr, and rmrmresonance peaks times 5000. The intensities used in the calculations arenormalized to the total number of monomers in the sample. Methods formeasuring 2,1 regio defects/10,000 monomers and 1,3 regio defects/10,000monomers follow standard methods. Additional references include Grassi,A. et. al. Macromolecules, 1988, 21, 617-622 and Busico et.al.Macromolecules, 1994, 27, 7538-7543. The average meso runlength=10000/[(stereo defects/10000 C)+(2,1-regio defects/10000C)+(1,3-regio-defects/10000 C)].

For some samples, polymer end-group analysis was determined by ¹H NMRusing a Varian Unity+400 MHz instrument run with a single 30° flipangle, RF pulse. 120 pulses with a delay of 8 seconds between pulseswere signal averaged. The polymer sample was dissolved in heatedd₂-1,1,2,2-tetrachloroethane and signal collection took place at 120° C.Vinylenes were measured as the number of vinylenes per 1000 carbon atomsusing the resonances between 5.55-5.31 ppm. Trisubstituted end-groups(“trisubs”) were measured as the number of trisubstituted groups per1000 carbon atoms using the resonances between 5.30-5.11 ppm. Vinylend-groups were measured as the number of vinyls per 1000 carbon atomsusing the resonances between 5.13-4.98 ppm. Vinylidene end-groups weremeasured as the number of vinylidenes per 1000 carbon atoms using theresonances between 4.88-4.69 ppm. The values reported in Table 1 are %vinylene, % trisubstituted (% trisub), % vinyl and % vinylidene wherethe percentage is relative to the total olefinic unsaturation per 1000carbon atoms.

Polymerization results are collected in Tables 1, 2 and 3 below. “Ex#”stands for example number. Under the Ex# column heading, the followingabbreviations are defined: PP=polypropylene, EP=ethylene-propylene;CPP=comparative polypropylene, CEP=comparative ethylene-propylene,Examples starting with a “C” as in CPP and CEP are comparative examples.“Cat ID” identifies the pre-catalyst used in the experiment.Corresponding numbers identifying the pre-catalyst are located above.Comparative pre-catalysts are named with a “C” followed by a dash and aletter, such as C-A. An asterisk next to the Cat ID number wouldindicate that the pre-catalyst was pre-alkylated with 20 equivalents ofTiBAl. “Act ID” identifies the activator used. “A” corresponds to MAO,“B” corresponds to dimethylanilinium tetrakisperfluorophenylborate, and“C” corresponds to dimethylanilinium tetrakisperfluoronaphthylborate.“Cat (μmol)” is the amount of pre-catalyst added to the reactor. For allexperiments using MAO as the activator, the molar ratio ofactivator/pre-catalyst was 500. For all experiments using borateactivators B or C, the molar ratio of activator/pre-catalyst was 1.1.T(° C.) is the polymerization temperature which was typically maintainedwithin +/−1° C. “Yield” is polymer yield, and is not corrected forcatalyst residue. “Quench time (s)” is the actual duration of thepolymerization run in seconds. “Quench Value (psi)” for ethylene basedpolymerization runs is the set maximum amount of ethylene uptake(conversion) for the experiment. For propylene homopolymerization orethylene-propylene copolymerizations runs, quench value indicates themaximum set pressure loss (conversion) during the polymerization.

TABLE 1 Propylene polymerization & Ethylene-propylene copolymerizationexamples. Quench quench Activity Cat Act Cat Isohexane Toluene T C2Value time yield (g P/mmol Ex# ID ID (umol) (uL) (uL) (° C.) (psig)(psi) (s) (g) cat · hr) PP-1 2 B 0.025 3869 231 70 0 15 32 0.24081,070,222 PP-2 2 B 0.025 3869 231 70 0 15 29 0.2728 1,345,315 PP-3 2 B0.025 3869 231 70 0 15 36 0.3330 1,317,363 EP-1 2 B 0.025 3849 231 70 1015 25 0.3019 1,738,944 EP-2 2 B 0.025 3829 231 70 20 15 22 0.30531,971,444 EP-3 2 B 0.025 3829 231 70 20 15 24 0.3097 1,897,736 EP-4 2 B0.025 3809 231 70 40 15 17 0.3197 2,740,286 EP-5 2 B 0.025 3809 231 7040 15 18 0.3268 2,614,400 EP-6 2 B 0.025 3789 231 70 60 15 17 0.32182,758,286 EP-7 2 B 0.025 3789 231 70 60 15 14 0.3330 3,425,143 EP-8 2 B0.025 3769 231 70 80 15 16 0.3254 2,928,600 EP-9 2 B 0.025 3769 231 7080 15 14 0.3459 3,662,471 PP-4 2 B 0.012 3916 184 70 0 15 73 0.1714700,545 PP-5 2 B 0.012 3916 184 70 0 15 79 0.2490 946,768 PP-6 2 B 0.0123916 184 100 0 15 92 0.1555 504,870 PP-7 2 B 0.012 3916 184 100 0 15 680.1661 738,222 PP-8 2 B 0.015 3895 205 70 0 15 66 0.2865 1,041,818 PP-92 B 0.015 3895 205 70 0 15 64 0.2663 1,003,328 PP-10 2 B 0.015 3895 205100 0 15 88 0.1681 457,415 PP-11 2 B 0.015 3895 205 100 0 15 79 0.1815550,000 PP-12 2 C 0.012 3916 184 70 0 15 90 0.2335 779,199 PP-13 2 C0.012 3916 184 70 0 15 113 0.2297 610,904 PP-14 2 C 0.012 3916 184 100 015 138 0.1663 360,999 PP-15 2 C 0.012 3916 184 100 0 15 73 0.1971814,463 PP-16 2 C 0.015 3895 205 70 0 15 243 0.1566 154,986 PP-17 2 C0.015 3895 205 70 0 15 142 0.1520 256,180 PP-18 2 C 0.015 3895 205 100 015 88 0.1644 446,840 PP-19 2 C 0.015 3895 205 100 0 15 66 0.1983 723,283PP-20 12 B 0.020 3790 310 70 0 20 154 0.2265 264,054 PP-21 12 B 0.0203790 310 70 0 20 159 0.1751 198,226 EP-10 12 B 0.020 3770 310 70 10 20100 0.2047 368,460 EP-11 12 B 0.020 3770 310 70 10 20 112 0.1877 302,471EP-12 12 B 0.020 3750 310 70 20 20 93 0.1998 385,054 EP-13 12 B 0.0203750 310 70 20 20 91 0.2064 409,163 EP-14 12 B 0.020 3730 310 70 40 2075 0.2028 486,072 EP-15 12 B 0.020 3730 310 70 40 20 74 0.2148 523,194EP-16 12 B 0.020 3710 310 70 60 20 55 0.2453 810,165 EP-17 12 B 0.0203710 310 70 60 20 58 0.2615 811,552 EP-18 12 B 0.020 3690 310 70 80 2047 0.2873 1,112,129 EP-19 12 B 0.020 3690 310 70 80 20 43 0.28601,200,000 PP-22 14 B 0.020 3790 310 70 0 20 144 0.2353 293,310 PP-23 14B 0.020 3790 310 70 0 20 156 0.2393 275,585 PP-24 14 B 0.040 3832 268 700 15 98 0.2318 212,228 PP-25 14 B 0.040 3832 268 70 0 15 96 0.2349220,448 PP-26 14 B 0.040 3832 268 100 0 15 107 0.1530 129,296 PP-27 14 B0.040 3832 268 100 0 15 64 0.1855 260,452 EP-20 14 B 0.020 3770 310 7010 20 78 0.2129 492,571 EP-21 14 B 0.020 3770 310 70 10 20 68 0.2240589,474 EP-22 14 B 0.020 3750 310 70 20 20 61 0.2170 644,554 EP-23 14 B0.020 3750 310 70 20 20 66 0.2364 648,659 EP-24 14 B 0.020 3730 310 7040 20 64 0.2327 653,448 EP-25 14 B 0.020 3730 310 70 40 20 52 0.2404835,367 EP-26 14 B 0.025 3855 205 70 40 15 79 0.1662 301,421 EP-27 14 B0.025 3855 205 70 40 15 46 0.1978 624,632 EP-28 14 B 0.025 3855 205 10040 15 53 0.1552 422,473 EP-29 14 B 0.025 3855 205 100 40 15 45 0.1622520,196 EP-30 14 B 0.020 3710 310 70 60 20 55 0.2484 812,945 EP-31 14 B0.020 3710 310 70 60 20 50 0.2831 1,011,071 EP-32 14 B 0.025 3835 205 7060 15 50 0.2182 630,940 EP-33 14 B 0.025 3835 205 70 60 15 37 0.26861,039,742 EP-34 14 B 0.025 3835 205 100 60 15 35 0.1695 695,385 EP-35 14B 0.025 3835 205 100 60 15 31 0.1761 818,013 EP-36 14 B 0.020 3690 31070 80 20 41 0.2630 1,163,145 EP-37 14 B 0.020 3690 310 70 80 20 360.2650 1,336,134 PP-28 14 C 0.040 3832 268 70 0 15 289 0.1597 49,820PP-29 14 C 0.040 3832 268 70 0 15 202 0.1732 77,168 PP-30 14 C 0.0403832 268 100 0 15 149 0.1509 91,455 PP-31 14 C 0.040 3832 268 100 0 15182 0.1421 70,231 EP-38 14 C 0.025 3855 205 70 40 15 57 0.2299 576,753EP-39 14 C 0.025 3855 205 70 40 15 71 0.2006 409,736 EP-40 14 C 0.0253855 205 100 40 15 51 0.1450 413,465 EP-41 14 C 0.025 3855 205 100 40 1544 0.1710 564,771 EP-42 14 C 0.025 3835 205 70 60 15 35 0.2880 1,171,525EP-43 14 C 0.025 3835 205 100 60 15 48 0.1611 485,322 EP-44 14 C 0.0253835 205 100 60 15 51 0.1472 414,810 PP-32 16 B 0.012 3899 201 70 0 10111 0.1903 514,324 PP-33 16 B 0.012 3899 201 70 0 10 123 0.2105 513,415EP-45 16 B 0.012 3879 201 70 10 10 33 0.2823 2,589,908 EP-46 16 B 0.0123879 201 70 10 10 31 0.2501 2,436,039 EP-47 16 B 0.012 3859 201 70 20 1028 0.2713 2,927,698 EP-48 16 B 0.012 3859 201 70 20 10 28 0.28193,042,086 EP-49 16 B 0.012 3839 201 70 40 10 22 0.2818 3,808,108 EP-5016 B 0.012 3839 201 70 40 10 24 0.3049 3,827,197 EP-51 16 B 0.012 3819201 70 60 10 18 0.2868 4,861,017 EP-52 16 B 0.012 3819 201 70 60 10 180.3357 5,657,865 EP-53 16 B 0.012 3799 201 70 80 10 15 0.3107 6,052,597EP-54 16 B 0.012 3799 201 70 80 10 13 0.3002 6,874,809 CPP-1 C-A B 0.0203790 310 70 0 20 119 0.2449 372,000 CPP-2 C-A B 0.020 3790 310 70 0 20133 0.2616 354,578 CEP-1 C-A B 0.020 3770 310 70 10 20 92 0.1996 390,098CEP-2 C-A B 0.020 3770 310 70 10 20 106 0.2013 341,830 CEP-3 C-A B 0.0203750 310 70 20 20 99 0.1781 323,491 CEP-4 C-A B 0.020 3750 310 70 20 20101 0.1954 348,583 CEP-5 C-A B 0.020 3730 310 70 40 20 77 0.1900 443,005CEP-6 C-A B 0.020 3730 310 70 40 20 74 0.2010 488,919 CEP-7 C-A B 0.0203710 310 70 60 20 62 0.1996 581,359 CEP-8 C-A B 0.020 3710 310 70 60 2067 0.2271 612,864 CEP-9 C-A B 0.020 3690 310 70 80 20 44 0.1503 619,085CEP-10 C-A B 0.020 3690 310 70 80 20 45 0.1803 722,806 CPP-3 C-B B 0.0203790 310 70 0 20 158 0.2327 265,943 CPP-4 C-B B 0.020 3790 310 70 0 20159 0.2146 243,096 CEP-11 C-B B 0.020 3770 310 70 10 20 107 0.1954328,097 CEP-12 C-B B 0.020 3770 310 70 10 20 97 0.2165 400,926 CEP-13C-B B 0.020 3750 310 70 20 20 85 0.2107 448,298 CEP-14 C-B B 0.020 3750310 70 20 20 75 0.2229 533,537 CEP-15 C-B B 0.020 3730 310 70 40 20 760.2110 503,046 CEP-16 C-B B 0.020 3730 310 70 40 20 67 0.2206 589,139CEP-17 C-B B 0.020 3710 310 70 60 20 57 0.2388 752,785 CEP-18 C-B B0.020 3710 310 70 60 20 59 0.2460 756,923 CEP-19 C-B B 0.020 3690 310 7080 20 43 0.2672 1,129,014 CEP-20 C-B B 0.020 3690 310 70 80 20 41 0.27011,197,488 CPP-5 C-C B 0.080 3664 436 70 0 12 2423 0.1071 1,989 CPP-6 C-CB 0.080 3664 436 70 0 12 2215 0.1037 2,107 CEP-21 C-C B 0.040 3812 26870 10 12 1212 0.0795 5,905 CEP-22 C-C B 0.040 3812 268 70 10 12 9300.0778 7,531 CEP-23 C-C B 0.040 3792 268 70 20 12 676 0.0807 10,741CEP-24 C-C B 0.040 3792 268 70 20 12 576 0.0812 12,688 CEP-25 C-C B0.040 3772 268 70 40 12 327 0.0761 20,932 CEP-26 C-C B 0.040 3772 268 7040 12 324 0.0779 21,619 CEP-27 C-C B 0.040 3752 268 70 60 12 221 0.076931,317 CEP-28 C-C B 0.040 3752 268 70 60 12 206 0.0777 33,897 CEP-29 C-CB 0.040 3732 268 70 80 12 160 0.0825 46,319 CEP-30 C-C B 0.040 3732 26870 80 12 169 0.0840 44,813 CPP-7 C-D B 0.025 3869 231 70 0 12 209 0.1795123,438 CPP-8 C-D B 0.025 3869 231 70 0 12 191 0.1721 130,023 CEP-31 C-DB 0.025 3849 231 70 10 12 130 0.1845 205,000 CEP-32 C-D B 0.025 3849 23170 10 12 81 0.2568 457,098 CEP-33 C-D B 0.025 3829 231 70 20 12 1210.1647 195,683 CEP-34 C-D B 0.025 3829 231 70 20 12 182 0.1248 98,580CEP-35 C-D B 0.025 3809 231 70 40 12 42 0.2829 969,943 CEP-36 C-D B0.025 3809 231 70 40 12 49 0.3139 926,262 CEP-37 C-D B 0.025 3789 231 7060 12 103 0.1457 203,302 CEP-38 C-D B 0.025 3789 231 70 60 12 34 0.27701,183,620 CEP-39 C-D B 0.025 3769 231 70 80 12 39 0.2553 942,646 CEP-40C-D B 0.025 3769 231 70 80 12 32 0.3078 1,402,633 CPP-9 C-E B 0.015 3843257 70 0 20 66 0.3674 1,346,198 CPP-10 C-E B 0.015 3843 257 70 0 20 710.3655 1,237,236 CPP-11 C-E B 0.015 3843 257 70 0 20 72 0.3585 1,195,000CPP-12 C-E B 0.015 3843 257 70 0 20 71 0.3706 1,261,617 CEP-41 C-E B0.015 3803 257 70 40 20 22 0.3874 4,169,327 CEP-42 C-E B 0.015 3803 25770 40 20 22 0.3980 4,422,222 CEP-43 C-E B 0.015 3803 257 70 40 20 230.3957 4,183,612 CEP-44 C-E B 0.015 3803 257 70 40 20 22 0.39274,363,333 CEP-45 C-E B 0.015 3763 257 70 80 20 17 0.4360 6,048,555CEP-46 C-E B 0.015 3763 257 70 80 20 17 0.4172 5,855,439 CEP-47 C-E B0.015 3763 257 70 80 20 19 0.4824 6,224,516 CEP-48 C-E B 0.015 3763 25770 80 20 21 0.3735 4,372,683 CPP-13 C-F B 0.080 3580 520 70 0 20 830.2652 143,438 CPP-14 C-F B 0.080 3580 520 70 0 20 84 0.2887 154,661CEP-49 C-F B 0.020 3875 205 70 10 20 98 0.1914 350,122 CEP-50 C-F B0.020 3875 205 70 10 20 106 0.2207 374,420 CEP-51 C-F B 0.020 3855 20570 20 20 78 0.2103 487,809 CEP-52 C-F B 0.020 3855 205 70 20 20 840.2063 444,719 CEP-53 C-F B 0.020 3835 205 70 40 20 46 0.2231 867,343CEP-54 C-F B 0.020 3835 205 70 40 20 57 0.2344 740,211 CEP-55 C-F B0.020 3815 205 70 60 20 46 0.2233 883,385 CEP-56 C-F B 0.020 3815 205 7060 20 35 0.2408 1,252,717 CEP-57 C-F B 0.020 3795 205 70 80 20 30 0.25161,509,600 CEP-58 C-F B 0.020 3795 205 70 80 20 27 0.2481 1,672,584CPP-15 C-G B 0.02 3895 205 70 0 15 112 0.2269 364,335 CPP-16 C-G B 0.023895 205 70 0 15 132 0.2082 283,265 CEP-59 C-G B 0.02 3875 205 70 10 1565 0.2344 654,140 CEP-60 C-G B 0.02 3875 205 70 10 15 56 0.2693 871,835CEP-61 C-G B 0.02 3855 205 70 20 15 54 0.2493 834,089 CEP-62 C-G B 0.023855 205 70 20 15 55 0.2478 813,942 CEP-63 C-G B 0.02 3835 205 70 40 1564 0.2212 620,187 CEP-64 C-G B 0.02 3835 205 70 40 15 41 0.28961,268,321 CEP-65 C-G B 0.02 3815 205 70 60 15 48 0.2622 979,170 CEP-66C-G B 0.02 3815 205 70 60 15 60 0.2375 714,883 CEP-67 C-G B 0.02 3795205 70 80 15 46 0.2484 982,681 CEP-68 C-G B 0.02 3795 205 70 80 15 360.3227 1,636,225 C2 Tm % % % % Ex# Mn Mw PDI (wt %) (° C.) vinylenetrisub vinyl vinylidene PP-1 9,638 28,402 2.95 141.3 0.0 7.2 79.3 13.5PP-2 9,852 27,279 2.77 140.7 1.1 2.6 81.6 14.7 PP-3 8,027 26,634 3.32140.6 0.0 1.5 83.8 14.7 EP-1 9,950 34,071 3.42 6.7 100.3 0.8 1.6 82.615.1 EP-2 10,701 38,543 3.60 11.2 90.1 0.0 1.5 83.1 15.4 EP-3 10,16738,311 3.77 9.4 91.9 0.0 1.1 85.1 13.8 EP-4 9,576 41,253 4.31 14.6 0.00.9 84.5 14.5 EP-5 9,235 40,154 4.35 13.6 0.0 1.4 84.6 13.9 EP-6 9,30144,887 4.83 15.3 0.6 2.3 82.7 14.3 EP-7 9,096 42,947 4.72 17.4 0.8 2.982.1 14.2 EP-8 10,427 51,822 4.97 19.2 1.2 4.3 80.9 13.7 EP-9 9,14749,408 5.40 27.8 1.9 7.8 77.5 12.8 PP-4 23,592 45,180 1.92 146.7 0.0 8.574.4 17.1 PP-5 19,627 43,962 2.24 145.8 4.6 5.5 77.1 12.8 PP-6 5,82310,579 1.82 138.7 0.7 2.6 88.8 7.9 PP-7 5,585 9,840 1.76 136.8 0.6 5.185.0 9.3 PP-8 15,798 39,708 2.51 144.8 2.5 14.4 66.9 16.3 PP-9 15,23039,075 2.57 144.3 0.0 2.4 87.4 10.2 PP-10 5,606 10,137 1.81 138.0 1.03.2 89.0 6.8 PP-11 4,809 9,027 1.88 136.0 1.4 3.8 87.9 6.9 PP-12 31,70466,032 2.08 147.9 0.0 10.6 80.3 9.1 PP-13 34,261 68,830 2.01 148.2 2.316.3 73.3 8.1 PP-14 8,493 15,276 1.80 140.9 0.0 0.9 93.6 5.6 PP-15 6,72012,807 1.91 138.0 1.0 2.1 92.8 4.1 PP-16 69,487 119,005 1.71 152.0 3.716.7 59.3 20.4 PP-17 49,419 90,662 1.83 150.4 0.0 11.3 75.5 13.2 PP-186,371 11,709 1.84 137.6 0.9 2.2 93.2 3.7 PP-19 5,813 11,048 1.90 136.50.0 1.8 94.4 3.9 PP-20 34,622 49,928 1.44 139.4 0.0 0.0 54.5 45.5 PP-2133,780 48,236 1.43 139.7 0.0 14.0 56.1 29.8 EP-10 26,816 42,824 1.60 8.596.2 1.2 0.0 51.2 47.6 EP-11 28,678 45,051 1.57 9.0 100.2 2.6 15.7 41.740.0 EP-12 28,359 45,205 1.59 11.1 0.0 0.0 51.9 48.1 EP-13 28,717 46,2581.61 9.1 3.3 4.4 47.8 44.4 EP-14 33,914 55,114 1.63 15.4 0.0 1.4 48.650.0 EP-15 30,289 50,468 1.67 13.4 0.0 1.1 54.4 44.4 EP-16 28,818 51,6431.79 17.6 1.0 10.3 45.4 43.3 EP-17 25,971 47,922 1.85 16.6 1.1 5.3 52.641.1 EP-18 21,946 48,382 2.20 20.6 0.9 3.5 44.2 51.3 EP-19 23,068 47,2232.05 20.4 1.0 2.9 53.3 42.9 PP-22 23,015 34,305 1.49 137.5 1.8 4.4 67.326.5 PP-23 21,775 32,897 1.51 137.7 3.2 8.0 64.0 24.8 PP-24 12,96026,637 2.06 136.1 0.0 6.7 64.0 29.3 PP-25 13,465 26,822 1.99 136.8 2.86.8 63.8 26.6 PP-26 4,143 6,698 1.62 123.3 1.1 11.7 70.0 17.2 PP-273,947 6,552 1.66 122.8 1.1 4.3 71.2 23.4 EP-20 20,710 32,957 1.59 3.01.4 5.8 65.5 27.3 EP-21 21,367 33,415 1.56 6.1 92.1 1.4 2.8 66.0 29.8EP-22 18,690 30,217 1.62 8.7 84.5 2.5 1.2 66.0 30.2 EP-23 17,875 29,9921.68 8.9 84.8 0.6 3.0 65.1 31.3 EP-24 24,261 40,211 1.66 13.7 84.2 1.43.6 63.8 31.2 EP-25 22,976 38,365 1.67 12.8 2.1 4.1 62.8 31.0 EP-2626,727 51,710 1.93 12.9 4.9 13.0 50.4 31.7 EP-27 20,556 41,140 2.00 15.83.5 11.1 57.6 27.8 EP-28 6,548 12,395 1.89 19.3 0.5 2.2 69.5 27.7 EP-296,251 11,881 1.90 19.2 0.5 1.8 69.6 28.1 EP-30 21,929 39,968 1.82 21.00.9 4.6 62.0 32.4 EP-31 18,133 35,440 1.95 20.3 118.7 0.0 0.8 64.1 35.2EP-32 22,011 49,009 2.23 18.9 3.0 9.8 57.1 30.1 EP-33 15,005 38,214 2.5518.9 3.6 19.8 55.3 21.3 EP-34 6,499 13,213 2.03 25.0 1.5 6.1 67.6 24.7EP-35 6,333 13,207 2.09 24.6 0.0 0.5 70.8 28.6 EP-36 16,660 48,598 2.9225.7 137.9 0.0 1.7 65.0 33.3 EP-37 16,087 39,315 2.44 26.9 0.0 3.9 64.132.0 PP-28 31,451 54,060 1.72 139.5 1.4 5.6 80.6 12.5 PP-29 28,04748,549 1.73 138.2 0.0 0.0 88.0 12.0 PP-30 5,681 9,837 1.73 124.7 0.7 2.789.6 7.0 PP-31 5,323 9,264 1.74 125.4 1.3 3.7 87.1 7.9 EP-38 28,03062,608 2.23 17.2 3.6 7.1 75.0 14.3 EP-39 34,179 71,414 2.09 18.2 3.318.7 69.2 8.8 EP-40 11,078 21,485 1.94 22.1 1.8 3.1 85.1 10.1 EP-418,349 16,728 2.00 20.3 1.3 2.5 88.6 7.6 EP-42 22,419 59,214 2.64 19.03.0 11.2 71.6 14.2 EP-43 11,508 24,271 2.11 27.8 2.6 7.0 80.9 9.6 EP-4412,324 24,099 1.96 27.8 1.7 6.7 82.1 9.6 PP-32 47,429 82,418 1.74 151.50.0 13.0 75.9 11.1 PP-33 42,074 78,314 1.86 150.7 7.6 21.5 62.0 8.9EP-45 17,652 56,954 3.23 8.8 100.3 2.0 4.7 78.7 14.7 EP-46 16,256 54,2873.34 8.3 104.5 0.0 0.0 86.9 13.1 EP-47 16,632 61,724 3.71 11.4 91.3 2.55.7 77.2 14.6 EP-48 16,261 63,177 3.89 12.8 90.0 2.5 5.5 79.1 12.9 EP-4915,300 65,806 4.30 16.1 2.3 5.7 78.2 13.8 EP-50 14,261 70,657 4.95 15.32.6 7.2 76.3 13.9 EP-51 13,162 82,508 6.27 21.0 1.5 7.8 77.9 12.7 EP-5213,629 87,474 6.42 19.8 1.9 6.1 77.8 14.2 EP-53 12,831 98,154 7.65 25.21.7 7.3 73.2 17.9 EP-54 13,417 97,515 7.27 24.4 1.4 4.5 79.1 15.0 CPP-125,220 53,948 2.14 138.7 3.3 4.4 37.8 54.4 CPP-2 28,677 44,260 1.54138.4 5.3 7.4 38.9 48.4 CEP-1 32,880 52,880 1.61 3.6 105.8 2.4 1.2 40.056.5 CEP-2 28,858 47,365 1.64 8.0 100.2 1.0 3.1 39.8 56.1 CEP-3 34,38354,039 1.57 9.5 88.9 0.0 4.7 38.8 56.5 CEP-4 30,928 52,200 1.69 9.7 89.52.1 3.2 37.9 56.8 CEP-5 36,261 60,943 1.68 13.4 3.3 4.4 36.7 55.6 CEP-635,037 58,905 1.68 13.6 4.3 3.3 35.9 56.5 CEP-7 30,348 53,280 1.76 20.7112.7 3.2 11.7 35.1 50.0 CEP-8 30,461 236,939 7.78 28.7 111.2 1.9 4.839.0 54.3 CEP-9 29,857 55,730 1.87 27.4 115.7 1.2 4.9 35.4 58.5 CEP-1023,616 116,202 4.92 23.1 115.7 1.1 4.4 37.8 56.7 CPP-3 27,587 40,1801.46 138.9 3.6 5.5 52.7 38.2 CPP-4 34,671 48,766 1.41 140.9 2.7 19.531.9 46.0 CEP-11 29,431 45,421 1.54 6.8 97.3 1.3 2.5 38.8 57.5 CEP-1225,567 41,455 1.62 9.5 93.7 0.0 2.3 40.2 57.5 CEP-13 26,490 42,679 1.6110.3 2.2 2.2 38.7 57.0 CEP-14 23,326 38,249 1.64 8.4 0.9 0.0 44.0 55.0CEP-15 32,878 53,423 1.62 14.1 0.0 0.0 39.7 60.3 CEP-16 27,356 47,0931.72 15.2 1.1 2.3 40.9 55.7 CEP-17 29,236 52,558 1.80 18.0 0.0 2.4 40.557.1 CEP-18 27,041 49,550 1.83 15.3 1.1 3.2 41.1 54.7 CEP-19 21,70448,769 2.25 20.5 0.8 4.2 45.0 50.0 CEP-20 22,483 47,343 2.11 22.0 0.01.8 55.8 42.5 CPP-5 3,643 5,514 1.51 * 0.5 1.7 41.5 56.3 CPP-6 3,5715,343 1.50 * 0.5 1.8 41.8 56.0 CEP-21 5,418 9,627 1.78 23.6 0.6 4.6 32.562.3 CEP-22 5,502 9,939 1.81 20.4 1.0 5.0 34.3 59.8 CEP-23 7,184 13,0351.81 25.6 0.0 2.5 36.0 61.5 CEP-24 6,673 12,081 1.81 24.2 0.0 3.7 37.359.0 CEP-25 13,406 22,369 1.67 41.9 0.0 3.9 39.0 57.1 CEP-26 13,10921,678 1.65 45.0 0.4 6.1 38.2 55.3 CEP-27 21,359 32,888 1.54 53.5 0.08.9 37.0 54.1 CEP-28 20,742 34,206 1.65 46.6 0.0 9.5 38.1 52.4 CEP-2925,915 41,693 1.61 55.2 0.9 8.5 36.8 53.8 CEP-30 26,539 41,978 1.58 54.90.0 7.6 38.1 54.3 CPP-7 89,641 147,267 1.64 141.8 6.7 20.0 20.0 53.3CPP-8 90,190 147,358 1.63 142.0 5.6 24.1 24.1 46.3 CEP-31 109,130182,358 1.67 8.1 0.0 5.0 10.0 85.0 CEP-32 59,009 113,096 1.92 6.3 95.72.1 0.0 10.6 87.2 CEP-33 117,536 197,873 1.68 13.2 4.4 0.0 8.9 86.7CEP-34 143,952 238,408 1.66 14.9 4.1 14.3 12.2 69.4 CEP-35 60,933122,443 2.01 17.4 0.0 8.0 20.0 72.0 CEP-36 48,758 110,165 2.26 15.8 5.64.2 16.7 73.6 CEP-37 129,035 218,743 1.70 19.6 4.2 4.2 10.4 81.3 CEP-3831,549 98,597 3.13 16.8 1.1 0.0 22.0 76.9 CEP-39 67,240 153,942 2.2927.5 3.3 8.3 16.7 71.7 CEP-40 35,389 115,893 3.27 24.5 2.2 6.7 23.3 67.8CPP-9 47,237 100,374 2.12 148.4 CPP-10 63,174 137,415 2.18 153.5 5.237.1 37.1 20.6 CPP-11 58,584 129,890 2.22 152.9 CPP-12 48,120 109,2032.27 150.7 5.4 29.8 35.1 29.8 CEP-41 24,197 64,519 2.67 14.72 67.1CEP-42 26,709 67,617 2.53 14.94 76.4 0.0 8.3 31.0 60.7 CEP-43 23,27466,644 2.86 14.04 77.5 CEP-44 21,988 57,691 2.62 12.47 106.0 3.9 18.235.4 42.5 CEP-45 20,590 64,503 3.13 23.61 96.3 CEP-46 21,840 62,130 2.8423.16 128.5 0.5 4.3 36.2 59.0 CEP-47 46,028 79,578 1.73 20.37 67.1CEP-48 33,243 72,847 2.19 27.47 72.7 2.0 4.6 28.9 64.5 CPP-13 2,3703,132 1.32 * 0.4 3.1 82.2 14.2 CPP-14 2,484 3,346 1.35 * 0.4 3.3 82.114.2 CEP-49 3,636 5,510 1.52 9.7 0.3 2.2 79.4 18.2 CEP-50 3,439 5,1971.51 12.0 0.4 2.8 79.1 17.7 CEP-51 3,391 5,593 1.65 12.3 0.6 3.1 79.317.0 CEP-52 4,024 6,458 1.60 18.0 0.6 3.0 77.9 18.5 CEP-53 3,750 7,1981.92 26.2 0.5 3.1 79.2 17.2 CEP-54 3,780 7,637 2.02 23.1 3.2 12.9 25.858.1 CEP-55 4,870 10,844 2.23 32.6 0.3 3.4 78.2 18.0 CEP-56 3,978 9,8052.46 34.0 0.4 3.5 80.3 15.8 CEP-57 4,585 12,093 2.64 41.7 0.4 3.7 80.415.6 CEP-58 4,170 11,438 2.74 38.9 0.6 3.9 80.0 15.5 CPP-15 79119127,194 1.61 0.0 131.9 11.2 35.5 27.1 26.2 CPP-16 95396 159,909 1.68 0.0132.4 10.2 38.7 23.4 27.7 CEP-59 70215 121,316 1.73 11.5 5.2 8.6 15.570.7 CEP-60 54250 106,170 1.96 8.1 10.9 38.3 22.9 27.9 CEP-61 59336111,783 1.88 13.3 3.9 44.8 26.6 24.7 CEP-62 51925 104,164 2.01 13.7 7.936.7 23.7 31.7 CEP-63 97237 160,132 1.65 19.0 5.5 30.9 16.4 47.3 CEP-6459697 120,679 2.02 14.0 8.7 33.7 22.1 35.6 CEP-65 67534 124,730 1.8522.5 6.8 13.7 16.4 63.0 CEP-66 97677 169,756 1.74 26.3 3.4 28.8 16.950.8 CEP-67 86449 154,485 1.79 30.6 3.4 18.6 16.9 61.0 CEP-68 45696117,956 2.58 24.4 7.1 25.3 24.2 43.4 *Polypropylene produced exhibitedno melting peak (non-crystalline)

TABLE 2 Propylene polymerization examples Quench quench Activity Cat ActCatalyst Iso-hexane Toluene T value time yield (g P/mmol Tm Ex# ID ID(umol) (uL) (uL) (C.) (psi) (s) (g) cat · hr) Mn Mw PDI (° C.) PP-34  2B 0.040 3832 268 70 15 26 0.3011 1,050,349 5,856 20,187 3.45 138.5 PP-35 2 B 0.040 3832 268 70 15 31 0.3400 977,636 5,239 17,503 3.34 136.9PP-36  2 B 0.040 3832 268 70 15 29 0.3622 1,135,819 4,819 14,888 3.09135.4 PP-37  2 B 0.040 3832 268 70 15 21 0.2954 1,290,583 6,856 23,4573.42 138.9 PP-38  2 B 0.040 3832 268 70 15 28 0.2871 913,039 7,31326,069 3.56 140.4 PP-39  2 B 0.040 3832 268 70 15 28 0.2700 870,9686,707 27,166 4.05 139.0 PP-40  2 B 0.040 3832 268 100 15 19 0.26441,245,864 3,563 6,500 1.82 130.1 PP-41  2 B 0.040 3832 268 100 15 190.2565 1,221,429 3,821 7,304 1.91 132.6 PP-42  2 B 0.040 3832 268 100 1519 0.2544 1,224,385 3,317 5,839 1.76 130.8 PP-43  2 B 0.040 3832 268 10015 23 0.2624 1,022,338 3,509 6,987 1.99 132.6 PP-44  2 B 0.040 3832 268100 15 31 0.2190 642,020 3,654 6,859 1.88 133.8 PP-45  2 B 0.040 3832268 100 15 25 0.2398 863,280 3,781 7,333 1.94 134.2 PP-46  7 A 0.050 04099 70 8 835 0.0617 5,321 50,959 76,581 1.50 149.5 PP-47  7 A 0.050 04099 70 8 892 0.0612 4,941 52,441 79,829 1.52 149.9 PP-48  7 A 0.050 04099 70 8 944 0.065 4,959 56,232 84,346 1.50 150.0 PP-49  7 A 0.050 04099 100 8 574 0.0544 6,821 13,376 20,509 1.53 141.6 PP-50  7 A 0.050 04099 100 8 591 0.0525 6,400 12,253 19,016 1.55 141.2 PP-51  7 A 0.050 04099 100 8 692 0.052 5,408 11,035 17,207 1.56 140.3 PP-52  8 A 0.025 04099 70 8 1801 0.0408 3,263 71,643 106,093 1.48 149.7 PP-53  8 A 0.025 04099 70 8 1801 0.0409 3,271 83,262 124,778 1.50 150.5 PP-54  8 A 0.025 04099 70 8 1801 0.0379 3,031 77,423 120,414 1.56 150.0 PP-55  8 A 0.025 04099 100 8 1800 0.0233 1,864 22,912 33,633 1.47 143.9 PP-56  8 A 0.025 04099 100 8 1801 0.0329 2,631 23,497 34,715 1.48 143.4 PP-57  8 A 0.025 04099 100 8 1801 0.0341 2,727 24,694 36,270 1.47 143.4 PP-58  8 A 0.040 04099 70 8 1121 0.0513 4,117 55,638 87,066 1.56 150.7 PP-59  8 A 0.040 04099 70 8 1396 0.0533 3,436 42,485 67,921 1.60 150.0 PP-60  8 A 0.040 04099 70 8 1366 0.0582 3,835 56,639 90,914 1.61 150.5 PP-61  8 A 0.040 04099 100 8 1067 0.0538 4,539 16,990 25,991 1.53 143.8 PP-62  8 A 0.040 04099 100 8 968 0.0532 4,947 17,327 26,356 1.52 144.0 PP-63  8 A 0.040 04099 100 8 1026 0.0548 4,808 16,488 25,228 1.53 144.4 PP-64  9 A 0.080 04098 70 8 552 0.0651 5,308 51,514 81,114 1.57 148.9 PP-65  9 A 0.080 04098 70 8 523 0.0586 5,038 59,629 94,591 1.59 149.4 PP-66  9 A 0.080 04098 70 8 664 0.0711 4,821 58,135 91,911 1.58 149.5 PP-67  9 A 0.080 04098 100 8 427 0.062 6,537 14,137 21,965 1.55 140.1 PP-68  9 A 0.080 04098 100 8 393 0.0645 7,389 13,714 21,792 1.59 140.6 PP-69  9 A 0.080 04098 100 8 431 0.0592 6,181 13,623 21,521 1.58 141.5 PP-70 10 A 0.080 04098 70 8 1802 0.0242 604 24,604 36,518 1.48 PP-71 10 A 0.080 0 4098 708 1800 0.0219 547 24,181 35,607 1.47 PP-72 10 A 0.080 0 4098 70 8 18030.0232 579 24,870 36,781 1.48 PP-73 10 A 0.080 0 4098 100 8 1803 0.0238594 7,222 11,004 1.52 PP-74 10 A 0.080 0 4098 100 8 1800 0.0216 5406,821 10,182 1.49 PP-75 10 A 0.080 0 4098 100 8 1803 0.0232 579 7,14510,737 1.50 PP-76 11 A 0.080 3609 489 70 20 1801 0.1411 3,526 50,58576,740 1.52 139.6 PP-77 11 A 0.080 3609 489 70 20 1802 0.1241 3,09952,762 80,621 1.53 140.4 PP-78 11 A 0.080 3609 489 70 20 1801 0.15813,950 56,598 85,261 1.51 140.4 PP-79 11 A 0.080 3609 489 100 20 14450.1336 4,161 7,328 12,324 1.68 124.9 PP-80 11 A 0.080 3609 489 100 201520 0.1338 3,960 9,000 14,460 1.61 128.4 PP-81 11 A 0.080 3609 489 10020 1458 0.1342 4,142 8,976 14,426 1.61 128.5 PP-82 12 A 0.080 3609 48970 20 1801 0.1590 3,973 55,140 83,420 1.51 140.9 PP-83 12 A 0.080 3609489 70 20 1654 0.1747 4,754 54,728 102,854 1.88 140.8 PP-84 12 A 0.0803609 489 70 20 1773 0.1720 4,366 57,908 89,070 1.54 141.1 PP-85 12 A0.080 3609 489 100 20 1281 0.1321 4,642 10,115 17,366 1.72 129.5 PP-8612 A 0.080 3609 489 100 20 1475 0.1335 4,072 10,701 15,303 1.43 128.3PP-87 12 A 0.080 3609 489 100 20 1522 0.1299 3,842 11,272 15,855 1.41129.9 PP-88 12 B 0.080 3720 380 70 20 41 0.3537 385,387 6,887 19,0012.76 129.9 PP-89 12 B 0.080 3720 380 70 20 43 0.3610 377,791 5,99316,559 2.76 130.2 PP-90 12 B 0.080 3720 380 70 20 39 0.3489 403,6126,689 17,935 2.68 130.4 PP-91 12 B 0.080 3720 380 100 20 34 0.2827376,376 3,461 5,361 1.55 119.0 PP-92 12 B 0.080 3720 380 100 20 330.2885 395,808 3,411 5,254 1.54 117.6 PP-93 12 B 0.080 3720 380 100 2025 0.2913 516,083 3,776 6,124 1.62 119.3 PP-94 13 A 0.080 3609 489 70 201800 0.1312 3,279 36,426 54,657 1.50 138.9 PP-95 13 A 0.080 3609 489 7020 1801 0.1291 3,225 41,306 62,787 1.52 139.7 PP-96 13 A 0.080 3609 48970 20 1801 0.1336 3,338 39,208 58,188 1.48 139.3 PP-97 13 A 0.080 3609489 100 20 1802 0.1295 3,234 6,917 10,918 1.58 126.0 PP-98 13 A 0.0803609 489 100 20 1802 0.1341 3,348 7,006 11,116 1.59 126.2 PP-99 13 A0.080 3609 489 100 20 1800 0.1272 3,180 5,808 9,189 1.58 121.9 PP-100 14A 0.080 3609 489 70 20 1802 0.1510 3,771 39,412 56,896 1.44 139.7 PP-10114 A 0.080 3609 489 70 20 1801 0.1410 3,523 33,934 66,447 1.96 139.8PP-102 14 A 0.080 3609 489 70 20 1800 0.1457 3,642 38,471 58,638 1.52140.5 PP-103 14 A 0.080 3609 489 100 20 1473 0.1306 3,991 8,266 11,8951.44 128.5 PP-104 14 A 0.080 3609 489 100 20 1489 0.1344 4,062 8,52111,812 1.39 127.8 PP-105 14 A 0.080 3609 489 100 20 1522 0.1299 3,8407,257 11,284 1.55 127.0 PP-106 14 B 0.080 3720 380 70 20 49 0.3424315,738 6,577 15,820 2.41 130.4 PP-107 14 B 0.080 3720 380 70 20 460.3445 334,106 7,045 17,506 2.48 130.1 PP-108 14 B 0.080 3720 380 70 2045 0.3417 338,689 7,452 18,124 2.43 130.8 PP-109 14 B 0.080 3720 380 10020 33 0.2777 382,156 3,416 5,071 1.48 120.4 PP-110 14 B 0.080 3720 380100 20 38 0.2740 321,932 3,104 4,424 1.43 117.5 PP-111 14 B 0.080 3720380 100 20 30 0.2807 418,262 3,351 4,867 1.45 118.0 PP-112 15 A 0.025 04099 70 8 406 0.0826 29,289 105,329 144,351 1.37 151.7 PP-113 15 A 0.0250 4099 70 8 366 0.0953 37,485 95,651 135,662 1.42 151.7 PP-114 15 A0.025 0 4099 70 8 389 0.0835 30,934 104,351 143,392 1.37 151.7 PP-115 15A 0.025 0 4099 100 8 613 0.056 13,165 18,362 25,732 1.40 145.9 PP-116 15A 0.025 0 4099 100 8 261 0.0756 41,647 18,791 25,940 1.38 143.6 PP-11715 A 0.025 0 4099 100 8 249 0.0782 45,206 17,827 25,938 1.45 144.7PP-118 16 A 0.025 0 4099 70 8 610 0.0606 14,313 105,751 158,433 1.50151.4 PP-119 16 A 0.025 0 4099 70 8 658 0.0641 14,026 122,794 174,1761.42 152.3 PP-120 16 A 0.025 0 4099 70 8 559 0.0615 15,843 123,532173,849 1.41 152.3 PP-120 16 A 0.025 0 4099 100 8 349 0.0612 25,25921,182 30,514 1.44 144.8 PP-122 16 A 0.025 0 4099 100 8 264 0.058331,860 20,286 29,401 1.45 144.3 PP-123 16 A 0.025 0 4099 100 8 3430.0616 25,899 18,540 29,074 1.57 144.5 PP-124 16 A 0.060 0 4099 70 8 1150.1654 86,146 60,601 98,968 1.63 149.5 PP-125 16 A 0.060 0 4099 70 8 1160.1599 82,707 61,400 99,289 1.62 149.7 PP-126 16 A 0.060 0 4099 70 8 1070.1428 79,851 58,934 95,808 1.63 150.5 PP-127 16 A 0.060 0 4099 100 8 730.1311 108,198 10,899 18,738 1.72 141.2 PP-128 16 A 0.060 0 4099 100 873 0.1247 103,200 10,859 18,741 1.73 142.2 PP-129 16 A 0.060 0 4099 1008 64 0.1258 117,387 10,612 18,319 1.73 141.7 PP-130 16 B 0.025 3881 21870 8 57 0.2885 735,292 20,485 47,051 2.30 146.4 PP-131 16 B 0.025 3881218 70 8 62 0.2963 691,527 23,036 51,949 2.26 147.1 PP-132 16 B 0.0253881 218 70 8 63 0.2903 666,718 22,124 50,697 2.29 146.7 PP-133 16 B0.025 3881 218 100 8 37 0.2203 869,129 5,074 10,086 1.99 137.4 PP-134 16B 0.025 3881 218 100 8 35 0.2226 915,840 4,576 9,635 2.11 136.2 PP-13516 B 0.025 3881 218 100 8 36 0.2239 903,126 4,742 9,410 1.98 137.1PP-136 17 A 0.050 0 4099 70 8 844 0.0546 4,657 52,659 76,413 1.45 151.1PP-137 17 A 0.050 0 4099 70 8 1012 0.0627 4,460 60,653 86,614 1.43 150.1PP-138 17 A 0.050 0 4099 70 8 940 0.0547 4,192 65,487 92,107 1.41 151.9PP-139 17 A 0.050 0 4099 100 8 935 0.0518 3,991 10,812 15,855 1.47 141.0PP-140 17 A 0.050 0 4099 100 8 954 0.0523 3,948 10,294 15,546 1.51 140.5PP-141 17 A 0.050 0 4099 100 8 991 0.0515 3,742 10,167 15,047 1.48 140.5PP-142 18 A 0.040 0 4099 70 8 1177 0.0686 5,246 63,766 93,574 1.47 151.0PP-143 18 A 0.040 0 4099 70 8 1013 0.0567 5,036 58,765 86,242 1.47 151.3PP-144 18 A 0.040 0 4099 70 8 1232 0.0531 3,879 61,768 90,088 1.46 151.3PP-145 18 A 0.040 0 4099 100 8 718 0.056 7,015 13,883 21,142 1.52 141.5PP-146 18 A 0.040 0 4099 100 8 701 0.0508 6,526 13,814 20,698 1.50 142.2PP-147 18 A 0.040 0 4099 100 8 760 0.0521 6,169 13,427 20,250 1.51 142.6PP-148 18 A 0.050 0 4099 70 8 604 0.068 8,102 57,334 84,281 1.47 151.4PP-149 18 A 0.050 0 4099 100 8 443 0.0652 10,592 14,456 21,744 1.50141.3 PP-150 18 A 0.050 0 4099 100 8 475 0.0622 9,428 13,889 20,847 1.50142.2 PP-151 18 A 0.050 0 4099 100 8 464 0.0644 10,000 13,614 20,7981.53 141.7 PP-152  18* B 0.030 3874 226 70 8 1800 0.0091 607 na na na naPP-153  18* B 0.030 3874 226 70 8 1802 0.0246 1,638 98,962 174,084 1.76151.8 PP-154  18* B 0.030 3874 226 70 8 1800 0.0119 793 89,066 156,4101.76 152.2 CPP-17 C-G B 0.020 3890 210 70 20 158 0.2669 303,871 89,355130,826 1.46 153.0 CPP-18 C-G C 0.020 3890 210 70 20 221 0.2052 167,056208,101 314,564 1.51 138.1 CPP-19 C-G B 0.020 3890 210 100 20 131 0.1877257,712 30,808 45,450 1.48 150.6 CPP-20 C-G C 0.020 3890 210 100 20 1960.1479 136,174 60,720 92,275 1.52 117.7 CPP-21 C-E B 0.020 3890 210 7020 84 0.3463 740,309 72,499 133,715 1.84 153.7 CPP-22 C-E C 0.020 3890210 70 20 101 0.3276 581,538 108,372 200,085 1.85 154.5 CPP-23 C-E C0.020 3890 210 100 20 86 0.2328 486,690 47,269 74,021 1.57 147.8 “na”indicates that the data was not available

TABLE 3 ¹³C NMR data for select polypropylene examples Cat Act mmrm +Ex# ID ID m r mmmm mmmr rmmr mmrr rmrr rmrm PP-34 2 B 0.974 0.026 0.93710.0240 0.0000 0.0221 0.0035 0.0000 PP-39 2 B 0.960 0.040 0.8430 0.06360.0317 0.0271 0.0009 0.0150 PP-40 2 B 0.965 0.035 0.9172 0.0327 0.00070.0295 0.0000 0.0000 PP-44 2 B 0.922 0.078 0.7799 0.0724 0.0311 0.03150.0139 0.0309 PP-46-48 7 A 0.930 0.070 0.8320 0.0312 0.0363 0.01530.0341 0.0125 PP-49-51 7 A 0.923 0.077 0.7939 0.0632 0.0303 0.02160.0289 0.0205 PP-58-60 8 A 0.969 0.031 0.9037 0.0461 0.0107 0.00200.0069 0.0085 PP-64-66 9 A 0.950 0.050 0.8320 0.0738 0.0166 0.02470.0181 0.0121 PP-67-69 9 A 0.904 0.096 0.7479 0.0935 0.0255 0.04250.0227 0.0085 PP-78 11 A 0.926 0.074 0.8090 0.0666 0.0104 0.0521 0.01580.0112 PP-79 11 A 0.942 0.057 0.8420 0.0584 0.0096 0.0418 0.0134 0.0096PP-83 12 A 0.975 0.035 0.9203 0.0254 0.0110 0.0271 0.0068 0.0030 PP-8612 A 0.933 0.067 0.8631 0.0292 0.0020 0.0436 0.0239 0.0100 PP-89 12 B0.929 0.072 0.8413 0.0453 0.0034 0.0478 0.0159 0.0134 PP-92 12 B 0.8640.137 0.7165 0.0653 0.0068 0.0706 0.0409 0.0383 PP-94 13 A 0.958 0.0420.8874 0.0420 0.0077 0.0293 0.0075 0.0059 PP-97 13 A 0.929 0.071 0.81440.0638 0.0126 0.0452 0.0171 0.0146 PP-102 14 A 0.961 0.039 0.9169 0.02090.0013 0.0267 0.0122 0.0048 PP-105 14 A 0.937 0.063 0.8587 0.0421 0.00200.0438 0.0121 0.0126 PP-106 14 B 0.930 0.070 0.8460 0.0441 0.0021 0.04650.0162 0.0135 PP-110 14 B 0.870 0.130 0.7281 0.0661 0.0045 0.0688 0.03680.0366 PP-112-114 15 A 0.851 0.149 0.8081 0.0076 0.0118 0.0017 0.00760.0387 PP-115-117 15 A 0.963 0.037 0.9020 0.0351 0.0127 0.0127 0.00400.0096 PP-124 16 A 0.982 0.018 0.9222 0.0371 0.0153 0.0056 0.0006 0.0088PP-127, 128 16 A 0.982 0.018 0.9159 0.0452 0.0127 0.0105 0.0001 0.0068PP-131 16 B 0.981 0.019 0.9214 0.0415 0.0100 0.0072 0.0025 0.0058 PP-13416 B 0.963 0.037 0.8502 0.0618 0.0281 0.0219 0.0070 0.0166 PP-136-138 17A 0.966 0.034 0.8648 0.0717 0.0167 0.0138 0.0060 0.0054 PP-142-144 18 A0.977 0.023 0.8865 0.0684 0.0094 0.0178 0.0041 0.0026 PP-145-147 18 A0.942 0.058 0.7602 0.1229 0.0267 0.0428 0.0127 0.0087 PP-148 18 A 0.9720.028 0.9280 0.0261 0.0074 0.0049 0.0099 0.0059 PP-149-151 18 A 0.9400.060 0.8399 0.0353 0.0367 0.0268 0.0160 0.0127 CPP-17 C-G B 0.938 0.0620.8377 0.0607 0.0068 0.0528 0.0111 0.0025 CPP-18 C-G C 0.961 0.0390.8890 0.0459 0.0048 0.0362 0.0068 0.0001 CPP-19 C-G B 0.894 0.1060.7293 0.0946 0.0135 0.0803 0.0227 0.0092 CPP-20 C-G C 0.921 0.0790.7939 0.0752 0.0092 0.0649 0.0153 0.0050 CPP-21 C-E B 0.986 0.0140.9500 0.0216 0.0064 0.0102 0.0031 0.0025 CPP-22 C-E C 0.990 0.0100.9576 0.0188 0.0068 0.0077 0.0031 0.0024 total stereo 2,1-regio 1,3regio ave. defects/ defects/ defects/ meso 10000 10000 10000 run Ex#rrrr mrrr mrrm monomer monomer monomer length PP-34 0.0005 0.0005 0.0123127.7 8.3 50.5 53.6 PP-39 0.0047 0.0019 0.0122 215.0 0.0 105.4 31.2PP-40 0.0010 0.0024 0.0166 147.6 0.0 94.0 41.4 PP-44 0.0202 0.00310.0170 381.5 0.0 74.4 21.9 PP-46-48 0.0086 0.0155 0.0146 306.4 10.3 12.330.4 PP-49-51 0.0092 0.0159 0.0164 352.7 0.0 14.4 27.2 PP-58-60 0.00560.0048 0.0118 85.4 23.6 18.0 78.7 PP-64-66 0.0067 0.0067 0.0094 271.918.7 12.0 33.0 PP-67-69 0.0170 0.0085 0.0340 359.1 0.0 55.2 24.1 PP-780.0027 0.0053 0.0269 395.5 8.0 90.0 20.3 PP-79 0.0014 0.0035 0.0201324.0 13.0 116.0 22.1 PP-83 0.0015 0.0018 0.0131 184.5 15.0 67.0 37.5PP-86 0.0019 0.0036 0.0227 387.5 1.0 57.0 22.4 PP-89 0.0035 0.00420.0253 385.5 8.0 92.0 20.6 PP-92 0.0102 0.0113 0.0401 749.0 1.0 94.011.8 PP-94 0.0019 0.0033 0.0151 213.5 12.0 80.0 32.7 PP-97 0.0034 0.00540.0237 384.5 4.0 117.0 19.8 PP-102 0.0012 0.0016 0.0144 218.5 9.0 50.036.0 PP-105 0.0024 0.0033 0.0230 342.5 4.0 117.0 21.6 PP-106 0.00260.0042 0.0248 381.0 4.0 91.0 21.0 PP-110 0.0090 0.0099 0.0403 711.0 1.099.0 12.3 PP-112-114 0.0665 0.0025 0.0556 239.9 0.0 0.0 41.7 PP-115-1170.0127 0.0016 0.0096 125.8 0.0 102.9 43.7 PP-124 0.0040 0.0008 0.005772.9 17.3 60.8 66.2 PP-127, 128 0.0032 0.0013 0.0044 83.4 4.4 106.0 51.6PP-131 0.0032 0.0023 0.0061 74.8 11.7 67.6 64.9 PP-134 0.0044 0.00090.0091 213.5 0.0 93.0 32.6 PP-136-138 0.0088 0.0029 0.0100 125.2 0.021.7 68.1 PP-142-144 0.0029 0.0007 0.0075 121.7 16.9 13.4 65.8PP-145-147 0.0067 0.0013 0.0180 312.9 0.0 35.9 28.7 PP-148 0.0069 0.00150.0094 103.6 0.0 0.0 96.5 PP-149-151 0.0088 0.0110 0.0127 275.3 0.0 17.834.1 CPP-17 0.0004 0.0010 0.0270 332.0 5.0 42.0 26.4 CPP-18 0.00000.0002 0.0170 215.5 17.0 37.0 37.1 CPP-19 0.0022 0.0039 0.0442 561.010.0 54.0 16.0 CPP-20 0.0013 0.0013 0.0338 426.0 7.0 55.0 20.5 CPP-210.0003 0.0010 0.0049 79.0 17.0 12.0 92.6 CPP-22 0.0004 0.0005 0.002966.0 24.0 13.0 97.1 **The following polymer samples were mixed for ¹³CNMR analysis: PP-46, 47, 48; PP-49, 50, 51; PP-58, 59, 60; PP-64, 65,66; PP67, 68, 69: PP-112, 113, 114; PP-115, 116, 117; PP-127, 128;PP-136, 137, 138; PP-142, 143, 144; PP-145, 146, 147; PP-149, 150, 151

Continuous stirred tank reactor runs: Polymerizations were carried outin a continuous stirred tank reactor. The reactor was either a 1-liter(for ethylene-propylene copolymerization runs) or a 0.5-liter (forpolypropylene runs) Autoclave reactor equipped with a stirrer, a watercooling/steam heating element with a temperature controller and apressure controller. The reactor was maintained at a pressure in excessof the bubbling point pressure of the reactant mixture to keep thereactants in the liquid phase. The reactors were operated liquid full.Isohexane (used as the solvent), and monomers (e.g., ethylene andpropylene) were purified over beds of alumina and molecular sieves.Toluene for preparing catalyst solutions was also purified by the sametechnique. All feeds were pumped into the reactors by a Pulsa feed pumpexcept for the ethylene which flowed as a gas under its own pressurethrough a Brooks flow controller. All liquid flow rates were controlledusing Brooks mass flow controller. Ethylene and propylene feeds werecombined into one stream and then mixed with a pre-chilled isohexanestream that had been cooled to at least 0° C. The mixture was fed intothe reactor through a single port.

An isohexane solution of tri-n-octyl aluminum (TNOA) (25 wt % in hexane,Sigma Aldrich) scavenger was added to the combined solvent and monomerstream just before it entered the reactor to further reduce any catalystpoisons. The feed rate of the scavenger solution was adjusted in a rangefrom 0 (no scavenger) to 1.5E-05 mole per minute to optimize catalystactivity.

The catalyst used wasrac-cyclotetramethylenesilylene-bis(2,4,7-trimethylinden-1-yl)hafniumdimethyl (2). The catalyst was activated with N,N-dimethylaniliniumtetrakis(heptafluoro-2-naphthyl)borate (C) at a molar ratio of about 1:1in 900 ml of toluene. The catalyst solution was then fed into thereactor through a separate port using an ISCO syringe pump.

The polymer produced in the reactor exited through a back pressurecontrol valve that reduced the pressure to atmospheric. This caused theunconverted monomers in the solution to flash into a vapor phase whichwas vented from the top of a vapor liquid separator. The liquid phase,comprising mainly polymer and solvent, was collected for polymerrecovery. The collected samples were first air-dried in a hood toevaporate most of the solvent, and then dried in a vacuum oven at atemperature of about 90° C. for about 12 hours. The vacuum oven driedsamples were weighed to obtain yields. The detailed polymerizationprocess conditions are listed in Table 4 for polypropylene runs and inTables 5 and 6 for ethylene-propylene copolymerization runs. Thescavenger feed rate and catalyst feed rate were adjusted to reach thetargeted conversion listed. All the reactions were carried out at apressure of about 2.4 MPa/g unless otherwise mentioned.

TABLE 4 Continuous stirred tank reactor runs making polypropyleneExample PP-152 PP-153 PP-154 Rxr T (C) 130 110 90 Catalyst/Activator 2/C2/C 2/C Cat (mol/min) 2.754E−07 2.754E−07 2.754E−07 Scavenger (mol/min)4.127E−06 4.127E−06 4.127E−06 Propylene (g/min) 14 14 14 polymer made(g) 136.5 154.6 229.9 Conversion (%) 48.8 55.2 82.1 Viscosity @190° C.(cp) 18 118 1380 Mn_DRI (g/mol) 1776 5222 13421 Mw_DRI (g/mol) 413613057 45422 Mz_DRI (g/mol) 7729 23260 89128 MWD (Mw/Mn) 2.33 2.5 3.38Mn_LS (g/mol) 3120 6152 15937 Mw_LS (g/mol) 4515 12438 48262 Mz_LS(g/mol) 9866 23552 106473 g′vis 0.792 0.892 0.769 Tc (° C.) 85.37 101.8102.6 Tm (° C.) 119.17 135.46 138.02 delta H (J/g) 74.34 95.43 94.91vinyl % 89.5 88.3 82.4 Vinyls/1000 C. 5.78 1.89 0.7 Vinylenes/1000 C.0.08 0.04 0 Vinylidenes/1000 C. 0.37 0.11 0.06 trisubstituted 0.23 0.10.09 olefin/1000 C *Conversion % = [(polymer yield)/(ethylene feed +propylene feed)] × 100

TABLE 5 Reactor conditions for continuous stirred tank teactor runsmaking ethylene-propylene copolymers Reactor Cat Polymer C2 C3 TpPressure Isohexane C3 C2 (micromol/ made Conversion conversionconversion Ex# (° C.) (psig) (g/min) (g/min) (SLPM) min) (gram) (%)*(%)* (%)* EP-55 100 350 55.2 14 0.3 0.220 144.6 50.4 80.5 49.7 EP-56 100350 55.2 14 0.5 0.184 136.5 46.9 73.1 45.8 EP-57 100 350 55.2 14 0.70.147 149.1 50.4 73.4 49.1 EP-58 100 350 55.2 14 0.9 0.147 150.1 50.066.6 48.8 EP-59 100 350 55.2 14 1.2 0.147 955.6 51.9 69.6 50.2 EP-60 100350 55.2 14 1.5 0.147 975.5 51.8 71.6 49.4 EP-61 70 350 55.2 14 0.30.220 235.4 82.1 95.8 81.8 EP-62 70 350 55.2 14 0.5 0.184 261.2 89.7122.9 88.4 EP-63 70 350 55.2 14 0.7 0.147 276.8 93.6 103.0 93.1 EP-64 70350 55.2 14 0.9 0.147 264.0 87.9 115.2 85.9 EP-65 70 350 55.2 14 1.20.147 265.0 86.3 70.4 87.8 EP-66 70 350 55.2 14 1.5 0.147 309.1 98.596.3 98.8 EP-67 70 350 55.2 14 0.9 0.064 252.8 84.2 84.1 84.2 EP-68 70350 55.2 14 0.9 0.039 186.9 62.2 69.2 61.7 *Conversion % = (polymeryield)/(ethylene feed + propylene feed) × 100; C2 conversion % =(polymer yield* ethylene content in polymer)/ethylene feed; C3Conversion × 100; C3% = (polymer yield*propylene content inpolymer)/propylene feed × 100

TABLE 6 Polymer characterization for continuous stirred tank reactorruns making ethylene-propylene copolymers Mn_DRI Mw_DRI Mz_DRI MWD Mn_LSMw_LS Ex# MFR (g/mol) (g/mol) (g/mol) (Mw/Mn) (g/mol) (g/mol) EP-557,303 24,707 46,460 3.38 EP-56 9,675 28,844 52,013 2.98 EP-57 11,27532,701 59,160 2.90 EP-58 11,602 31,085 55,150 2.68 EP-59 12,713 35,62764,113 2.80 EP-60 14,284 39,036 70,041 2.73 EP-61 49.5 66,216 219,352467,440 3.31 91,519 263,226 EP-62 30.7 73,270 227,591 454,742 3.1198,212 287,124 EP-63 20.6 66,330 232,080 489,332 3.50 94,544 279,874EP-64 22.0 72,201 234,559 481,610 3.25 95,998 293,704 EP-65 12.4 78,735242,525 504,757 3.08 104,616 297,373 EP-66 80.3 52,778 238,633 516,0424.52 78,451 368,579 EP-67 39.4 58,002 202,052 420,842 3.48 82,078270,159 EP-68 13.8 78,980 205,673 394,974 2.60 101,147 243,200 Mz_LS TmTg delta H Ethylene Vinyls/ vinyl Ex# (g/mol) g′_(vis) (° C.) (° C.)(J/g) (wt %) 1000 C. % EP-55 117.3 73.2 3.78 1.61 93.6 EP-56 105.1 −21.557.5 6.05 1.34 88.2 EP-57 97.4 −23.7 51.1 7.80 1.02 77.3 EP-58 87.5−27.1 43.4 9.03 1.04 85.2 EP-59 73.1 −37.0 35.7 11.85 0.91 85.0 EP-6056.1 −36.1 25.4 14.94 0.84 85.7 EP-61 520,510 0.740 130.0 74.3 2.76EP-62 599,668 0.747 119.0 65.4 5.32 EP-63 594,507 0.808 109.7 58.7 5.89EP-64 612,329 0.750 87.0 40.4 8.88 EP-65 606,298 0.762 100.9 49.6 7.21EP-66 913,528 0.559 77.1 −30.4 38.5 10.57 EP-67 588,915 0.707 101.7−22.3 56.9 6.77 0.18 38.3 EP-68 458,835 0.867 99.3 −23.1 49.2 7.54 0.1446.7

All documents described herein are incorporated by reference herein,including any priority documents and/or testing procedures to the extentthey are not inconsistent with this text, provided however that anypriority document not named in the initially filed application or filingdocuments is not incorporated by reference herein. As is apparent fromthe foregoing general description and the specific embodiments, whileforms of the invention have been illustrated and described, variousmodifications can be made without departing from the spirit and scope ofthe invention. Accordingly, it is not intended that the invention belimited thereby. Likewise, the term “comprising” is consideredsynonymous with the term “including” for purposes of Australian law.Likewise whenever a composition, an element or a group of elements ispreceded with the transitional phrase “comprising”, it is understoodthat we also contemplate the same composition or group of elements withtransitional phrases “consisting essentially of,” “consisting of”,“selected from the group of consisting of,” or “is” preceding therecitation of the composition, element, or elements and vice versa.

1. A process for polymerization, comprising: (i) contacting one or moremonomers comprising propylene and optionally ethylene, with a catalystsystem comprising a metallocene catalyst compound and an activator,wherein the metallocene catalyst compound is represented by the formula:

where each R³ is hydrogen; each R⁴ is independently a C₁-C₁₀ alkyl; eachR² and R⁷ is independently hydrogen, or C₁-C₁₀ alkyl, each R⁵ and R⁶ isindependently hydrogen, C₁-C₅₀ substituted or unsubstituted hydrocarbyl,or C₁-C₅₀ substituted or unsubstituted halocarbyl; and R⁴ and R⁵, R⁵ andR⁶ and/or R⁶ and R⁷ may optionally be bonded together to form a ringstructure; J is a bridging group represented by the formula Ra₂J′, whereJ′ is C or Si, and each Ra is, independently, C₁ to C₂₀ substituted orunsubstituted hydrocarbyl, and the two R^(a) form a cyclic structureincorporating J′ and the cyclic structure may be a saturated orpartially saturated cyclic or fused ring system; and each X is aunivalent anionic ligand, or two Xs are joined and bound to the metalatom to form a metallocycle ring, or two Xs are joined to form achelating ligand, a diene ligand, or an alkylidene ligand; and (ii)obtaining a polymer having: 1) greater than 40% vinyl chain ends,relative to the total unsaturated chain ends, 2) a Tm of 70° C. or more;3) an Mw of 3000 to 300,000 g/mol, and 4) a g′_(vis) of 0.90 or less. 2.The process of claim 1, wherein step (i) occurs at a temperature ofgreater than 60° C.
 3. The process of claim 1, wherein the polymerproduced has 1) greater than 70% vinyl chain ends, relative to totalunsaturated chain ends, and 2) an Mw of 3000 to 200,000 g/mol.
 4. Theprocess of claim 1, wherein the polymer produced is isotacticpolypropylene having a Tm of 115° C. or more.
 5. The process of claim 1,wherein the polymer produced is a propylene-ethylene copolymercontaining 30 wt % or less of ethylene.
 6. The process of claim 1,wherein the polyolefin produced has a g′_(vis) of 0.85 or less.
 7. Theprocess of claim 1, wherein the polyolefin produced has at least X %vinyl chain ends (relative to total unsaturations as measured by ¹H NMR,where X=47.8*g′_(vis)+45.1.
 8. The process of claim 1 wherein R², R⁴ andR⁷ are, independently, selected from the group consisting of methyl,ethyl, propyl, butyl, pentyl, heptyl, hexyl, octyl, nonyl, decyl and anisomers thereof
 9. The process of claim 1 wherein R² and R⁴ are,independently, a C₁ to C₁₀ alkyl.
 10. The process of claim 1 wherein R⁴and R⁷ are, independently, a C₁ to C₁₀ alkyl.
 11. The process of claim 1wherein each X is, independently, selected from the group consisting ofhydrocarbyl radicals having from 1 to 20 carbon atoms, hydrides, amides,alkoxides, sulfides, phosphides, halides, dienes, amines, phosphines,ethers, and a combination thereof, (two X′s may form a part of a fusedring or a ring system).
 12. The process of claim 1 wherein J isrepresented by the formula:

wherein J′ is a carbon or silicon atom, x is 1, 2, 3, or 4, and each R′is, independently, hydrogen or C₁-C₁₀ hydrocarbyl.
 13. The process ofclaim 1 wherein J is cyclopentamethylenesilylene,cyclotetramethylenesilylene, cyclotrimethylenesilylene.
 14. The processof claim 1 wherein the activator comprises alumoxane.
 15. The process ofclaim 1 wherein alumoxane is present at a molar ratio of aluminum tocatalyst compound transition metal of 100:1 or more.
 16. The process ofclaim 1 wherein the activator comprises a non-coordinating anionactivator.
 17. The process of claim 1 wherein activator is representedby the formula:(Z)_(d) ⁺(A^(d−)) wherein Z is (L-H) or a reducible Lewis Acid, L is anneutral Lewis base; H is hydrogen; (L-H)⁺ is a Bronsted acid; A^(d−) isa non-coordinating anion having the charge d−; and d is an integer from1 to
 3. 18. The process of claim 1 wherein activator is represented bythe formula:(Z)^(d+)(A^(d−)) wherein A^(d−) is a non-coordinating anion having thecharge d−; d is an integer from 1 to 3, and Z is a reducible Lewis acidrepresented by the formula: (Ar₃C⁺), where Ar is aryl or arylsubstituted with a heteroatom, a C₁ to C₄₀ hydrocarbyl, or a substitutedC₁ to C₄₀ hydrocarbyl.
 19. The process of claim 1 wherein the activatoris one or more of: N,N-dimethylaniliniumtetrakis(pentafluorophenyl)borate, triphenylcarbeniumtetrakis(pentafluorophenyl)borate, trimethylammoniumtetrakis(perfluoronaphthyl)borate, triethylammoniumtetrakis(perfluoronaphthyl)borate, N,N-dimethylaniliniumtetrakis(perfluoronaphthyl)borate, N,N-diethylaniliniumtetrakis(perfluoronaphthyl)borate, tropilliumtetrakis(perfluoronaphthyl)borate, triphenylcarbeniumtetrakis(perfluoronaphthyl)borate, triphenylphosphoniumtetrakis(perfluoronaphthyl)borate, triethylsilyliumtetrakis(perfluoronaphthyl)borate, benzene(diazonium)tetrakis(perfluoronaphthyl)borate, trimethylammoniumtetrakis(perfluorobiphenyl)borate, triethylammoniumtetrakis(perfluorobiphenyl)borate, tripropylammoniumtetrakis(perfluorobiphenyl)borate, tri(n-butyl)ammoniumtetrakis(perfluorobiphenyl)borate, tri(t-butyl)ammoniumtetrakis(perfluorobiphenyl)borate, N,N-dimethylaniliniumtetrakis(perfluorobiphenyl)borate, N,N-diethylaniliniumtetrakis(perfluorobiphenyl)borate,N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(perfluorobiphenyl)borate, tropilliumtetrakis(perfluorobiphenyl)borate, triphenylcarbeniumtetrakis(perfluorobiphenyl)borate, triphenylphosphoniumtetrakis(perfluorobiphenyl)borate, triethylsilyliumtetrakis(perfluorobiphenyl)borate, benzene(diazonium)tetrakis(perfluorobiphenyl)borate, [4-t-butyl-PhNMe₂H][(C₆F₃(C₆F₅)₂)₄B],trimethylammonium tetrakis(pentafluorophenyl)borate, tripropylammoniumtetrakis(pentafluorophenyl)borate, tri(n-butyl)ammoniumtetrakis(pentafluorophenyl)borate, N,N-dimethylaniliniumtetrakis(pentafluorophenyl)borate, N,N-diethylaniliniumtetrakis(pentafluorophenyl)borate, tropilliumtetrakis(pentafluorophenyl)borate, triphenylcarbeniumtetrakis(pentafluorophenyl)borate, triphenylphosphoniumtetrakis(pentafluorophenyl)borate, triethylsilyliumtetrakis(pentafluorophenyl)borate, benzene(diazonium)tetrakis(pentafluorophenyl)borate, trimethylammoniumtetrakis-(2,3,4,6-tetrafluorophenyl) borate, triethylammoniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, tripropylammoniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, tri(n-butyl)ammoniumtetrakis-(2,3,4,6-tetrafluoro-phenyl)borate, dimethyl(t-butyl)ammoniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-dimethylaniliniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-diethylaniliniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate,N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis-(2,3,4,6-tetrafluorophenyl)borate, tropilliumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylcarbeniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylphosphoniumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, triethylsilyliumtetrakis-(2,3,4,6-tetrafluorophenyl)borate, benzene(diazonium)tetrakis-(2,3,4,6-tetrafluorophenyl)borate, trimethylammoniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triethylammoniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tripropylammoniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tri(n-butyl)ammoniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tri(t-butyl)ammoniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-dimethylaniliniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-diethylaniliniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate,N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tropilliumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbeniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylphosphoniumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triethylsilyliumtetrakis(3,5-bis(trifluoromethyl)phenyl)borate, benzene(diazonium)tetrakis(3,5-bis(trifluoromethyl)phenyl)borate,tri(2,6-dimethylphenyl)phosphonium tetrakis(pentafluorophenyl)borate,triphenylcarbenium tetrakis(perfluorophenyl)borate,1-(4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluorophenyl)pyrrolidinium,tetrakis(pentafluorophenyl)borate,4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluoropyridine, andtriphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate). 20.The process of claim 1 wherein the process occurs at a temperature offrom about 0° C. to about 300° C., at a pressure in the range of fromabout 0.35 MPa to about 10 MPa, and at a time up to 300 minutes.
 21. Theprocess of claim 1 further comprising obtaining polymer having at least90% allyl chain ends.
 22. The process of claim 1 wherein the monomerscomprise ethylene and propylene.
 23. A polymer having: 1) greater than70% vinyl chain ends, relative to the total unsaturated chain ends; 2) aTm of 90° C. or more; 3) an Mw of 3000 to 200,000 g/mol; and 4) ag′_(vis) of 0.90 or less.
 24. A branched isotactic polypropylene polymerhaving at least X % vinyl chain ends (relative to total unsaturations asmeasured by ¹H NMR), where X=47.8*g′_(vis)+45.1.
 25. The polymer ofclaim 23 having greater than 80% vinyl unsaturation (relative to totalunsaturation as measured by ¹H NMR).
 26. The polymer of claim 23 havinga Mw of 3000 to 100,000 g/mol.
 27. The polymer of claim 23 having a Tmof 100° C. more.
 28. A branched ethylene-propylene copolymer having 1)20 wt % or less ethylene, 2) a Tm of 50° C. or more; and 3) greater than75% vinyl chain ends (relative to the total unsaturated chain ends). 29.The polymer of claim 28 having a Mw of 20,000 to 300,000 g/mol.